Mobile processing system for hazardous and radioactive isotope removal

ABSTRACT

A mobile processing system is disclosed for the removal of radioactive contaminants from nuclear process waste water. The system is fully scalable, modular, and portable allowing the system to be fully customizable according the site-specific remediation requirements. It is designed to be both transported and operated from standard sized intermodal containers or custom designed enclosures for increased mobility between sites and on-site, further increasing the speed and ease with which the system may be deployed. Additionally, the system is completely modular wherein the various different modules perform different forms or stages of waste water remediation and may be connected in parallel and/or in series. Depending on the needs of the particular site, one or more different processes may be used. In some embodiments, one or more of the same modules may be used in the same operation.

CROSS-REFERENCE TO RELATED APPLICATIONS

The present application is a divisional of U.S. Ser. No. 14/748,535,filed Jun. 24, 2015, entitled: MOBILE PROCESSING SYSTEM FOR HAZARDOUSAND RADIOACTIVE ISOTOPE REMOVAL, which claims priority to U.S.Provisional Ser. No. 62/016,517, filed Jun. 24, 2014, entitled: MOBILEPROCESSING SYSTEM FOR HAZARDOUS AND RADIOACTIVE ISOTOPE REMOVAL, whichare both herein incorporated by reference in their entireties.

The following related applications are expressly incorporated byreference in their entirety: Currently pending U.S. application Ser. No.13/850,890, filed Mar. 26, 2013 entitled SUBMERSIBLE FILTERS FOR USE INSEPARATING RADIOACTIVE ISOTOPES FROM RADIOACTIVE WASTE MATERIALS, andprovisional application 61/615,516, filed Mar. 26, 2012, to which Ser.No. 13/850,890 claims priority; Currently pending U.S. application Ser.No. 13/850,908, filed Mar. 26, 2013 entitled SELECTIVE REGENERATION OFISOTOPE-SPECIFIC MEDIA RESINS IN SYSTEMS FOR SEPARATION OF RADIOACTIVEISOTOPES FROM LIQUID WASTE MATERIALS, which also claims the benefit of61/615,516 previously listed above; Currently pending U.S. applicationSer. No. 13/863,206, filed Apr. 15, 2013 entitled ADVANCED TRITIUMSYSTEM FOR SEPARATION OF TRITIUM FROM RADIOACTIVE WASTES AND REACTORWATER IN LIGHT WATER SYSTEMS, and provisional application 61/320,515,filed Apr. 2, 2010, and U.S. application Ser. No. 13/079,331, PATENTAPPLICATION Provisional filed Apr. 4, 2011 entitled ADVANCED TRITIUMSYSTEM AND ADVANCED PERMEATION SYSTEM FOR SEPARATION OF TRITIUM FROMRADIOACTIVE WASTES AND REACTOR WATER both to which Ser. No. 13/863,206claims priority; and U.S. Provisional Application 62/016,517, filed Jun.24, 2014 entitled MOBILE PROCESSING SYSTEM FOR HAZARDOUS AND RADIOACTIVEISOTOPE REMOVAL, to which the present application also claims priority.

Applicant believes that some of the above-incorporated materialconstitutes “essential material” within the meaning of 37 CFR1.57(c)(1)-(3), applicants have amended the specification to expresslyrecite the essential material that has been incorporated by reference asallowed by the applicable rules.

FIELD OF THE INVENTION

This invention relates generally to nuclear waste remediation,specifically a mobile processing system for the removal of radioactivecontaminants from nuclear process waste water. The mobile system isfully scalable, able to accommodate massive-scope industrial nuclearwaste water cleanup projects worldwide, and transportable onconventional national and international transportation infrastructure.

BACKGROUND

With a worldwide need for abundant and inexpensive energy production,nuclear generated power is increasing exponentially along with worldpopulation growth. The first commercial nuclear power stations startedoperation in June 1954. Since then, nuclear power generation hasincreased such that there are over 443 commercial nuclear power reactorsoperable in 31 countries, with over 375,000 MWe total capacity.Currently, as of 2015, there are about 66 more reactors underconstruction. Increased nuclear power production requires an increase innuclear waste-water remediation.

With the present state of the art, nuclear waste water is typicallycontainerized and stored indefinitely at specialized storage facilities.What is needed in the art is a mobile, modular, and scalable waste watertreatment system designed to be both transported and operated from anintermodal shipping container for increased mobility, modularity, andscalability between sites and on-site, further increasing the speed,flexibility, and ease with which the system may be deployed.Additionally, a complete modular waste water treatment system is neededwherein various different modules for performing different forms ofwaste water remediation may be connected in parallel and/or in series inorder to perform all of the waste water remediation requirements andprocess time requirements for any given site. It would also beadvantageous for additional modules to be available for furtherprocessing of the contaminants removed from the water during the wastewater remediation process(es) such that the contaminants do not need tobe transported from the site for further processing prior to finaldisposition. An all-in-one mobile, modular, and scalable waste waterremediation and contaminant post-processing system as described in thisdisclosure would be advantageous for providing a complete solution forany given site, reducing transportation of hazardous materials, reducingimplementation costs, and diminishing overall complexity of standardexisting practices.

Mobile water processing is well known in the art. However, most existingmobile water processing systems are comprised of merely one specificprocess, or multiple processes within a single transportable module.Sites requiring waste water remediation are diverse in their specificrequirements, topography, and the location. Natural disaster, terroristattacks, and malfunctions often require rapid deployment of aid tomitigate overall damage to the environment and adverse effect to peopleliving in the region surrounding the site. Current water remediationsystems are not sufficient to perform this task. What is needed is ahighly mobile, easily transportable, scalable, modular system that canbe deployed quickly (often within 24 hours depending on site location,topography, and remediation requirements) and cost-effectively. Thesystem should be highly adaptable to differing remediation requirements,scalable to maximize efficiency, and modular to perform all remediationneeds including outputting water within safety standards as well asprocessing the removed contaminants to final disposition standards.

So as to reduce the complexity and length of the Detailed Specification,and to fully establish the state of the art in certain areas oftechnology, Applicant(s) herein expressly incorporate(s) by referenceall of the following publications identified below. Applicant(s)expressly reserve(s) the right to swear behind any of the incorporatedmaterials.

KUR-5P12-SDD-001 “Kurion Mobile Processing System” (KMPS), System LevelDesign Description, formerly marked Kurion Confidential, Document IssuedFeb. 9, 2014, filed Jun. 24, 2014 as U.S. Provisional Application62/016,517, which is herein incorporated by reference in its entirety.

Applicant(s) believe(s) that the material incorporated above is“non-essential” in accordance with 37 CFR 1.57, because it is referredto for purposes of indicating the background of the invention orillustrating the state of the art. However, if the Examiner believesthat any of the above-incorporated material constitutes “essentialmaterial” within the meaning of 37 CFR 1.57(c)(1)-(3), applicant(s) willamend the specification to expressly recite the essential material thatis incorporated by reference as allowed by the applicable rules.

DESCRIPTION OF RELATED ART

In a discussion of prior art, CN. Patent No. 101229949 issued Sep. 7,2011, titled MOBILE RADIOACTIVE LIQUID WASTE TREATMENT EQUIPMENTgenerally describes a movable treatment device for radioactive wastewater, which comprises a protecting vehicle, a heat preservation cabin,a treatment system of waste water, a PLC controlling system and anexternal connecting pipeline, wherein, the treatment system of wastewater consists of a liquid and solid separator, a pre-filter, anultra-filter, a security filter, a reverse osmosis filter of two levelsand a combined adsorption device; the PLC system consists of a PLC, aflow meter, a conductivity meter, a radioactivity detector and apressure controlling device. The invention solves the contradictionbetween the low interception and adsorption efficiency of nuclide andsmall size under the condition of large flow, meanwhile, which solvesthe problems of integration of a plurality of techniques and protectionof the movable treatment device of radioactive waste water and realizesautomatic operation, safety and reliability in the overall process. Whatthis patent does not disclose is a mobile treatment system designed tobe both transported and operated from a standard sized intermodalcontainer for increased mobility between sites and on-site, modularityin the ability to perform multiple different waste water remediationprocesses within separate modules, and system scalabilty of addingmultiple process-specific modules for quicker system process timesrequired for a given project.

In a discussion of prior art, U.S. Pat. No. 5,972,216 issued Oct. 26,1999, titled PORTABLE MULTI-FUNCTIONAL MODULAR WATER FILTRATION UNITgenerally describes a portable multi-functional modular water filtrationunit having configurable modules that can be adapted to renderenvironmental water potable or to isolate contaminants from groundwateror water from other sources such as backwash from reverse osmosis waterpurification units (ROWPU) or shower and laundry water (“gray water”)such that the water may be recycled or discharged in full compliancewith applicable laws. Plural treatment tanks as well as inlet and outletfilters may be coupled via pressure gauge bearing quick connect fittingsin series and parallel arrangements, to allow changes of filter elements(for replacement or substitution of a different active material) and toaccommodate flow in filtration arrays. The water purification systemspecifically addresses the changing water purifying needs that ariseduring troop deployment, training and maneuvers, disaster relief andenvironmental cleanup. What this patent does not disclose is a mobiletreatment system designed to be both transported and operated from astandard sized intermodal container for increased mobility between sitesand on-site, modularity in the ability to perform multiple differentwaste water remediation processes within separate modules, and systemscalabilty of adding multiple process-specific modules for quickersystem process times required for a given project.

In a discussion of prior art, U.S. patent application Ser. No.14/041,474 filed Sep. 30, 2013, titled MOBILE WATER FILTRATION UNIT ANDCONTROL SYSTEM, AND RELATED DEVICES, COMPONENTS, SYSTEMS AND METHODSgenerally describes a standardized, modular mobile water purificationunit for the production of safe potable water and for treatment ofwastewater is disclosed to fulfill the water need for humans, animalsand households. In one embodiment, the unit can be based on astandardized climate-controlled container that is robust both physicallyand functionally, can be easily transported and quickly set up in remoteregions and disaster areas. The unit may work for purification of waterof brackish, sea or polluted surface water, and of wastewater, and canbe customized to the given water type based on easy changeable treatmentmodules. The unit includes a rigid frame that can be removed from thecontainer, and also includes a control system for remote monitoring andcontrol of the unit. This application teaches away from operating awater treatment system from within an intermodal container.

BRIEF SUMMARY OF THE INVENTION

Although the best understanding of the present invention will be hadfrom a thorough reading of the specification and claims presented below,this summary is provided in order to acquaint the reader with some ofthe new and useful features of the present invention. Of course, thissummary is not intended to be a complete litany of all of the featuresof the present invention, nor is it intended in any way to limit thebreadth of the claims, which are presented at the end of the descriptionof this application.

The mobile processing system as disclosed is designed to be bothtransported and operated from standard sized intermodal containers orcustom designed enclosures for increased mobility between sites andon-site, further increasing the speed and ease with which the system maybe deployed. Additionally, the system is completely modular wherein thevarious different modules perform different forms of waste waterremediation and may be connected in parallel and/or in series in orderto perform all of the remediation requirements for any given site. Afurther advantage of the mobile processing system is the availability ofadditional modules for further processing of the contaminants removedfrom the water during the waste water remediation process(es) such thatthe contaminants do not need to be transported from the site for furtherprocessing prior to final disposition. An all-in-one mobile, modularwaste water remediation and contaminant post-processing system isextremely advantageous for providing a complete solution for any givensite, reducing transportation of hazardous materials, implementationcosts, and overall complexity of standard existing practices.

The mobile processing system encompasses multiple forms of waste waterprocessing. Depending on the needs of the particular site, one or moredifferent processes may be used. In some embodiments, one or more of thesame modules may be used in the same operation. For instance, two ormore separate ISM modules may be used in series wherein each module isoperative to remove a specific isotope from the waste stream. Anotherexample is placing two of the same module in parallel to handle anincreased flow capacity or to bring one module online while another isbrought offline for maintenance. For processes that take more time, suchas feed/blend, it may be advantageous to place one or more modules inparallel to reduce overall processing time.

In an embodiment, systems and methods are disclosed for a MobileProcessing System (MPS) water treatment process to remove radioactivecontaminants from nuclear process waste water and contaminatedgroundwater.

In an embodiment, systems and methods are disclosed for utilizingmodified transportable intermodal containers (one example: ISOcontainers) or custom designed containers (hereinafter all enclosurecontainers are referred to as skids unless otherwise specified) whichcontain components of various sub-systems of the processing system.Skids may remain on, and be operated from the trailers that were usedfor transporting the system to the treatment site, or they may beoffloaded and placed adjacent each other or stacked. An example of anintermodal container for use with the system is a modified ISO shippingcontainer; however, other containers that comply with regulations forconventional intermodal freight transport may be used.

In an embodiment, systems and methods are disclosed where the skids canbe connected in a variety of configurations to provide differentoperating modes or capacities as required to process a particularnuclear process waste water. As mentioned, each skid consists of anenclosed, modified intermodal container, which is further configuredwith a drip pan and leak detection. Process lines between skids mayconsist of hoses with double containment for the prevention of spills tothe environment.

In an embodiment, a system and method is provided for in situ (on-site)removal of radioactive material from nuclear facility process waterusing a fully scalable, portable, and modular system. In general, thedesign of the system and method can prevent the radioactive materialfrom leaking to the environment. Should the radioactive material beleaked from a train, dam installation, leak detector installation, orpiping installed in or outside the reactor building, etc., the systemwill have a design that can prevent the radioactive material fromdifusing, such as leak protection of the joints, etc. The design canprevent the retention of flammable gas, such as hydrogen gas, if suchretention is a matter of concern. The process system is designed forease of transfer from one site to another with flexibility for operatingin different modes of filtration and ion removal.

In an embodiment, systems and methods are disclosed for modularity andscalability of the system. Skids (process-specific modules) may be addedor removed allowing for a phased approach to site remediation. Quickerprocess times may be achieved by adding multiples of specific skids,depending on deadline requirements.

Aspects and applications of the invention presented here are describedbelow in the attachments and description of the invention. Unlessspecifically noted, it is intended that the words and phrases in thespecification and the claims be given their plain, ordinary, andaccustomed meaning to those of ordinary skill in the applicable arts.The inventors are fully aware that they can be their own lexicographersif desired. The inventors expressly elect, as their own lexicographers,to use only the plain and ordinary meaning of terms in the specificationand claims unless they clearly state otherwise and then further,expressly set forth the “special” definition of that term and explainhow it differs from the plain and ordinary meaning. Absent such clearstatements of intent to apply a “special” definition, it is theinventors' intent and desire that the simple, plain and ordinary meaningto the terms be applied to the interpretation of the specification andclaims.

The inventors are also aware of the normal precepts of English grammar.Thus, if a noun, term, or phrase is intended to be furthercharacterized, specified, or narrowed in some way, then such noun, term,or phrase will expressly include additional adjectives, descriptiveterms, or other modifiers in accordance with the normal precepts ofEnglish grammar. Absent the use of such adjectives, descriptive terms,or modifiers, it is the intent that such nouns, terms, or phrases begiven their plain, and ordinary English meaning to those skilled in theapplicable arts as set forth above.

Further, the inventors are fully informed of the standards andapplication of the special provisions of 35 U.S.C. § 112, 6. Thus, theuse of the words “function,” “means” or “step” in the DetailedDescription or Description of the Drawings or claims is not intended tosomehow indicate a desire to invoke the special provisions of 35 U.S.C.§ 112, 6, to define the invention. To the contrary, if the provisions of35 U.S.C. § 112, 6 are sought to be invoked to define the inventions,the claims will specifically and expressly state the exact phrases“means for” or “step for, and will also recite the word “function”(i.e., will state “means for performing the function of . . . ”, withoutalso reciting in such phrases any structure, material or act in supportof the function. Thus, even when the claims recite a “means forperforming the function of . . . ” or “step for performing the functionof . . . ”, if the claims also recite any structure, material or acts insupport of that means or step, or that perform the recited function,then it is the clear intention of the inventors not to invoke theprovisions of 35 U.S.C. § 112, 6. Moreover, even if the provisions of 35U.S.C. § 112, 6 are invoked to define the claimed inventions, it isintended that the inventions not be limited only to the specificstructure, material or acts that are described in the preferredembodiments, but in addition, include any and all structures, materialsor acts that perform the claimed function as described in alternativeembodiments or forms of the invention, or that are well known present orlater-developed, equivalent structures, material or acts for performingthe claimed function.

BRIEF DESCRIPTION OF THE DRAWINGS

A more complete understanding of the present invention may be derived byreferring to the detailed description when considered in connection withthe following illustrative figures. In the figures, like referencenumbers refer to like elements or acts throughout the figures.

FIG. 1 is an isometric view of an example embodiment Mobile ProcessingSystem comprising five separate skids.

FIG. 2 is a top view of the example embodiment system of FIG. 1.

FIG. 3 is a general diagram depicting the primary mechanical componentsof the example embodiment system of FIG. 1.

FIG. 4 is a legend describing mechanical component symbols.

FIG. 5 is a more detailed diagram depicting the primary mechanicalcomponents of the example embodiment system of FIG. 1.

FIG. 6 is a continuation of FIG. 5.

FIG. 7 is a diagram depicting the mechanical components of an exampleembodiment Control and Solids Feed skid.

FIG. 8 is a diagram depicting the mechanical components of an exampleembodiment Feed/Blend skid.

FIG. 9 is a diagram depicting the mechanical components of an exampleembodiment Solids Removal Filter skid.

FIG. 10 is a diagram depicting the mechanical components of an exampleembodiment Ultra Filter skid.

FIG. 11 is a diagram depicting the mechanical components of an exampleembodiment Ion Specific Media skid.

FIG. 12 is a diagram depicting the mechanical components of the IonSpecific Media vessel portion of the example embodiment Ion SpecificMedia skid of FIG. 11.

FIG. 13 is a diagram depicting the mechanical components in an exampleembodiment Sample Enclosure for an example Feed/Blend skid.

FIG. 14 is a diagram depicting the mechanical components in an exampleembodiment Sample Enclosure for an example embodiment Solids RemovalFilter skid.

FIG. 15 is a diagram depicting the mechanical components in an exampleembodiment Sample Enclosure for an example Ultra Filter skid.

FIG. 16 is a diagram depicting the mechanical components in an exampleembodiment Sample Enclosure for an example embodiment Ion Specific Mediaskid.

FIG. 17 depicts a typical gauge valve and PDIT manifold.

FIG. 18 is a legend describing instrumentation symbols.

FIG. 19 is a diagram depicting instrumentation and control of an exampleembodiment Control and Solids Feed skid.

FIG. 20 is a diagram depicting instrumentation and control of an exampleembodiment Feed/Blend skid.

FIG. 21 is a diagram depicting instrumentation and control of an exampleembodiment Solids Removal Filter skid.

FIG. 22 is a diagram depicting instrumentation and control of an exampleembodiment Ultra Filter skid.

FIG. 23 is a diagram depicting instrumentation and control of an exampleembodiment Ion Specific Media skid.

FIG. 24 is a diagram depicting instrumentation of the Ion Specific Mediavessel portion of the example embodiment Ion Specific Media skid of FIG.23.

FIG. 25 represents an embodiment of the Pilot skid as a smaller scalecomplete system.

FIG. 26A depicts a top view of a possible stacking configuration usingthree skids.

FIG. 26B depicts a top view of a possible stacking configuration usingfour skids.

FIG. 26C depicts a top view of a possible stacking configuration usingthree skids.

FIG. 26D depicts a side view of a possible stacking configuration usingtwo skids stacked end-to-end.

FIG. 27A depicts a top view of an example skid stacking configurationaccording to FIG. 26A.

FIG. 27B depicts a front view of the configuration of FIG. 27A.

Elements and acts in the figures are illustrated for simplicity and havenot necessarily been rendered according to any particular sequence orembodiment.

DETAILED DESCRIPTION

In the following description, and for the purposes of explanation,numerous specific details, process durations, and/or specific formulavalues are set forth in order to provide a thorough understanding of thevarious aspects of exemplary embodiments. It will be understood,however, by those skilled in the relevant arts, that the apparatus,systems, and methods herein may be practiced without these specificdetails, process durations, and/or specific formula values. It is to beunderstood that other embodiments may be utilized and structural andfunctional changes may be made without departing from the scope of theapparatus, systems, and methods herein. In other instances, knownstructures and devices are shown or discussed more generally in order toavoid obscuring the exemplary embodiments. In many cases, a descriptionof the operation is sufficient to enable one to implement the variousforms, particularly when the operation is to be implemented in software.It should be noted that there are many different and alternativeconfigurations, devices, and technologies to which the disclosedembodiments may be applied. The full scope of the embodiments is notlimited to the examples that are described below.

In the following examples of the embodiments, references are made to thevarious embodiments in which the invention may be practiced. It is to beunderstood that other embodiments may be utilized and structural andfunctional changes may be made without departing from the scope of theinvention.

System Overview

As previously discussed, the MPS equipment is contained in intermodalcontainers or skids. Example containers are ISO shipping containers,which are widely used standardized containers that can be quickly andeasily transported to sites around the world, as needed, on existinginfrastructure including truck, rail, ship, plane, and otherconventional industrial transportation mediums. Additionally, customdesigned enclosures may be used. For purposes of this disclosure, theMPS container(s) is (are) hereinafter referred to as a skid or skids.

Each skid is modified or customized to hold the process equipment, allowfor connection of interconnecting hoses, power and signal cables, andallow for removal of lids for filter and ISM vessels replacement. Theskids may be operated while mounted on transport trailers. Elevatedaccess platforms may be installed to allow disconnect of filters and ISMvessels for replacements, hydrogen venting, sampling, access to thecontrol room, and placement of interconnecting hoses. Crane access willbe required for routine operational replacement of solids removalfilters, ultra filters, and ISM vessels. Alternatively, openings in thesidewalls of skids, with or without doors, may be provided to affordforklift, or equivalent, access to filters and ISM vessels for thepurpose of routine operational replacement. Additionally, these skidscan be mounted on, and operated from, trailers on site to be easilymoved around, or rearranged, as needed. If custom designed containersare used, the resulting skid may have integral wheels and towingfixtures, thereby not relying on transport trailers for mobility. Inaddition to integral wheels, a custom designed skid may include a builtin transport-power-source and vehicle operating controls, i.e. a skidthat is drivable under its own power for purposes of mobility to andaround the site. In some embodiments, the system will be implemented asa permanent installation on the site.

Modularity

Modularity is a key aspect to effective, efficient, flexible, deployableremediation systems. Containing separate processes within separatemodules allows for better remediation customization—allowing only thenecessary processes to be brought on-site thus reducing shipping andprocess costs. At any time, processes may be added or removed allowingfor a phased approach to site remediation. Mobile processing modules aresimpler to transport, setup, and are more cost-efficient. Standardshipping sizes, such as intermodal containers, allow easy stacking forsimple cost-effective transport. Modularity also allows for simplersetup, as processes may be set up in any configuration as required bythe topography of the region, including stacking. Modularity also allowsfor easy skid replacement or simple phase out for skid maintenance. Eachmodule is equipped with standard sized quick disconnects for quick andsimple connection/disconnection between any skids in any configuration.

Scalability Size of Module:

Scalability is another key aspect to effective, efficient, deployableremediation systems. Using scaled modules that are appropriate for theneeds of a specific remediation site reduces costs of transport, setup,and operation. The modules in the depicted embodiment have been designedto fit in 6.1 m (20 ft) intermodal containers; however, other containersizes are possible. Number of Modules in Operation:

Some waste remediation sites may have tighter process time requirementsto meet deadlines. Sometimes, the scope of a given remediation projectmay be so massive that conventional configurations will not be capableof meeting the time constraints. In these situations, it would bebeneficial to bring in additional modules. It may even be beneficial tobring in more than one complete system to be used in unison eitherentirely separately or in parallel to increase processing rates and meetremediation deadlines.

Another distinguishing aspect of the mobile processing system is that itcan be used as a complete remediation solution. The mobile processingsystem isn't just for water remediation—it also includes the capabilityof processing the contaminants that are removed from the water duringthe remediation process. There are many technologies available forpreparing the removed contaminants for final disposition that aredescribed in detail in co-owned, co-pending patent applications whichare described below and incorporated by reference herein in theirentirety.

One such technology is vitrification. With vitrification, orglassification, frit is added to the contaminant or contaminant ladenslurry that is output from the water remediation process, as disclosedin U.S. patent application Ser. No. 12/985,862 ('862), filed Jan. 6,2011, entitled Microwave-Enhanced System for Pyrolysis and Vitrificationof Radioactive Waste, which is hereby incorporated by reference in itsentirety, and U.S. patent application Ser. No. 13/036,809 ('809), filedFeb. 28, 2011, entitled Advanced Microwave System for TreatingRadioactive Waste, which is hereby incorporated by reference in itsentirety.

Another technology for further processing of contaminants removed fromwaste water is volume reduction by separating ions from an ion exchangeresin with an elution agent and running through an inorganic ISM column,as disclosed in U.S. patent application Ser. No. 13/850,908 ('908),filed Mar. 26, 2013, entitled Selective Regeneration of Isotope-SpecificMedia Resins in Systems for Separation of Radioactive Isotopes fromLiquid Waste Materials, which is herein incorporated by reference in itsentirety.

For purposes of the present disclosure, the systems and methodsdisclosed in the '862, '809, and '908 US patent applications could beincluded in one or more intermodal containers or skids as described, andused in combination with skids disclosed herein.

For the following discussions, normal operations are termed “Mode D” asidentified in Table 1. In an embodiment, this mode has all five of thetreatment skids installed and operational.

FIG. 1 is an isometric view of an embodiment of a Mobile ProcessingSystem (MPS) comprising separate skids: a Control and Solids Feed skid140, a Feed/Blend skid 130, a Solids Removal Filter skid 120, an UltraFilter skid 110, and an Ion Specific Media (ISM) skid 100.

In an embodiment, the five skids depicted in FIG. 1 can be arranged infive different operation modes that allow for flexibility inaccommodating specific processing needs. In the depicted embodiment,control and solids feed functionalities are combined into a Control andSolids Feed Skid 140. In some embodiments there are six skids where thecontrol and solids feed functionalities are split in a Control skid anda separate Solids Feed skid. Control may occur entirely on site,remotely, or both. On-site control may occur entirely within a Controlskid or within a combined Control and Solids Feed Skid 140.Additionally, control may be augmented with one or more of remotecontrol from a remotely located control station or from mobile devicessuch as smart phones, tablets, and laptop computers. The five operationmodes are listed in Table 1. All operation modes are operated andmonitored by a control system.

TABLE 1 Operation Modes and Active Modules Operation Mode ModulesDescription MODE A Solids Removal Filter RO reject water is routed tothe skid 120 SRF and Ultra Filter skids, and Pump (P-250) Enabled thendirectly back to the storage Ultra Filter skid tanks. Pump (P-350)Enabled MODE B Solids Feed skid 140 RO reject water is routed throughFeed/Blend skid 130 the Feed/Blend system where Pump (P-150) Enabledmedia is added. Then it is routed Pump (P-152) Enabled through thefiltration skids and Solids Removal Filter back to the storage tanks.skid 120 Pump (P-250) Disabled Ultra Filter skid 110 Pump (P-350)Enabled MODE C Solids Removal Filter RO reject water is routed directlyskid 120 to the filtration skids, then the Pump (P-250) Enabled ISMvessel and back to the Ultra Filter skid 110 storage tanks. Pump (P-350)Enabled ISM skid 100 Pump (P-450) Enabled MODE D Solids Feed skid 140 ROreject water is routed through Feed/Blend skid 130 all of the systemswith media Pump (P-150) Enabled addition, filtration and ISM Pump(P-152) Enabled vessel Solids Removal Filter skid 120 Pump (P-250)Disabled Ultra Filter skid 110 Pump (P-350) Enabled ISM skid 100 Pump(P-450) Enabled MODE E ISM skid 100 RO reject water is routed directlyPump (P-450) Enabled through the ISM vessel and then to the storagetanks.

In the configuration depicted in an embodiment of FIG. 1, the skids arearranged in operation mode D to perform a water treatment process toremove radioactive contaminants from nuclear process waste water.Influent water from storage tanks is treated with a sorbent, filtered,and finally polished in columns using an ion specific media (ISM) toremove any residuals.

The mixed process water is then passed to the Solids Removal Filter skidwhere it is filtered through a solids removal filter (SRF) that collectsall of the sorbent solids and part of the waste solids. The filteredwater is then passed to the Ultra Filter skid where it is filtered againthrough an ultra-filter that collects the remainder of the colloidalsuspended solids. Finally, the ultra-filtered water is sent to the ISMskid where it is passed through ISM vessels that remove specific ionsfrom the feed water. After the water has been treated it is returned tothe storage tanks.

In an embodiment, a specialized ion exchange media or sorbent additiveis used to control the chemical properties of the process water enteringthe ISM vessels. In some embodiments the additive is in powder form. Thechemical properties of process water can vary significantly betweendifferent batches entering the system. The underlying chemical processin the ISM vessels is reliant on equilibrium therefore when the chemicalproperties of the influent to the ISM vessels changes, the columnefficiency could fluctuate. The quantity and type of sorbent additivecan be adjusted to normalize the concentration of an ion (Sr or Ca, forexample) such that the chemical conditions in the ISM vessels remainstable. In some embodiments, the chemical properties of the solutiongoing into the ISM vessels is monitored, automatically and/or manually,and the amount of sorbent additive is adjusted incrementally tostabilize any fluctuations. In alternative embodiments, in order tominimize the system adjustment response time, the chemical properties ofthe influent process water is monitored, automatically and/or manually,and the amount of sorbent additive is adjusted stoichiometrically. Thechemical properties in the ISM vessels may also be monitored toconfirm/fine tune the effect of the sorbent additive adjustment.

In an example embodiment, the MPS is used to treat reverse osmosis (RO)reject water containing strontium (Sr-90). A powdered sorbent (or otherion exchange material in powder form) is fed from the Control/SolidsFeed skid 140 into the Feed/Blend skid 130. The additive is mixed intothe process water and given time to absorb a particular isotope from thesolution. The sorption time is dependent on the ISM used and thetargeted isotope to be removed. In the example embodiment, to removeSr-90 from the RO reject water, the sorption time is about fortyminutes. In an alternative embodiment, other nuclear waste componentsbesides Sr-90 can be removed, and other waste water besides RO rejectwater can be treated.

In some embodiments, each skid includes climate control and shockabsorption to prevent damage to the hardware during transport, setup,and usage.

The depicted embodiment is an example of the preferred skid arrangementwherein the skids are situated proximately on a level surface in asingle layer (i.e. not stacked). For certain sites, the topography ofthe region may render the preferred skid arrangement unfeasible,therefore elevation, distance, and system footprint need to beconsidered. At these certain sites the skids may need to be placed atone or more of different elevations, farther distances apart, orstacked. In some embodiments additional pumps may be situated betweenthe skids, hose diameters may be increased or decreased, and/or othersystem component settings may be altered to achieve the desired pressureand flow conditions. In some embodiments, differences in elevation maybe used as a gravitational advantage to reduce pumping requirements andthus save on energy costs.

In one embodiment, for skids containing pumps, two or more pumps may beplaced in parallel at each pump location wherein each pump is configuredfor a differing range of pressures. Depending on the skid arrangement atthe particular site, the appropriate pump will be utilized. Placing twoor more pumps in parallel allows for a more highly mobile and modularsystem allowing the system to function at appropriate flow conditionsfor a wider range of differing site topographies and skid arrangements.

FIG. 2 is a top view of the system of FIG. 1 in operation mode D. In anembodiment, the five skids are depicted side by side but do notnecessarily have to be in this configuration on site. In an embodiment,the skids will need to be connected in the order shown to operate inoperation mode D, but may be positioned as required by the topography ofthe site.

FIG. 3 is a general diagram depicting the primary mechanical componentsof the system of FIG. 1. In an embodiment, the process is generallycontinuous, as shown. The water to be treated is piped from the storagetanks into the Feed/Blend skid 130. A powdered sorbent or ion exchangematerial is fed from the Control and Solids Feed skid 140 into theFeed/Blend skid 130. In the depicted embodiment the sorbent is fed froma Super Sack® (or equivalent industrial sack, bag or other packaging)into the hopper. From the hopper it is directed into an auger to controlfeed rate into another hopper which directs it to the Feed/Blend skid130.

In an embodiment, a first tank T-100 and second tank T-101 tank areconnected in series. A pre-determined quantity of the sorbent and apre-determined quantity of the contaminated water are combined in thefirst feed/blend tank T-100 and remain in first feed/blend tank T-100,with or without agitation, for a pre-determined period of timecalculated to allow the contaminant to be sorbed by the sorbent. Inorder to convert this batch process into a continuous process, thecontents of first feed/blend tank T-100 are transferred to the secondfeed/blend tank T-101 providing the source of a continuous flow oftreated water to be pumped from the Feed/Blend skid 130 into the SolidsRemoval Filter skid 120. Alternatively, the treated water may betransferred directly into the Solids Removal Filter skid 120 while thesecond feed/blend tank T-101 is being processed in parallel. In analternative embodiment (not shown), feed/blend tanks T-100 and T-101 areconnected in parallel. A pre-determined quantity of the sorbent and apre-determined quantity of the contaminated water are combined in thefirst feed/blend tank T-100 and remain in first feed/blend tank T-100,with or without agitation, for a pre-determined period of timecalculated to allow the contaminant to be sorbed by the sorbent. Thetreated water in first feed/blend tank T-100 is pumped at a ratecalculated to provide a continuous flow from the Feed/Blend skid 130into the Solids Removal Filter skid 120. At the time the treated waterstarts to flow from first feed/blend tank T-100, the filling process isstarted for second feed/blend tank T-101. The alternating use offeed/blend tanks T-100 and T-101 provides a steady and continuous flowof treated water to the Solids Removal Filter skid 120. Regardless ofwhether the tanks are configured in parallel or in series, the treatedwater delivered to the Solids Removal Filter skid 120 passes through afirst solids removal filter FLT-200 or a second solids removal filterFLT-201 (depending on which filter is online) to remove the sorbent andany other solids. Next the treated water is pumped into the Ultra Filterskid 110 where it is further filtered by a first ultra filter FLT-300 ora second ultra filter FLT-301 (depending on which filter is online).

Continuing with an embodiment description, from the Ultra Filter skid110 the process water is pumped into the Ion Specific Media skid 100where it is passed through one or more ion specific media (ISM) vesselscontaining ion exchange media specific to the removal requirements ofthe site. The depicted embodiment shows four ISM vessels VSL-460,VSL-461, VSL-462, and VSL-463, where three are online at a time and thefourth is in standby. Every five days, or on a different pre-determinedmaintenance schedule, the next vessel down the line is taken offline andthe standby vessel is put online. After passing through one or more ofthe ISM vessels the water is either returned to the storage tanks forfurther disposition or run through the system continuously until itmeets purity standards.

FIG. 4 is a legend describing the line types, mechanical componentsymbols, and abbreviations used in the subsequent figures.

FIGS. 5 and 6 depict a more detailed diagram of the primary mechanicalcomponents of the system of FIG. 1. Circles labeled with “S” indicatelocations where samples will be taken. The circles connected with dashedlines indicate instrumentation that may be implemented to provide datafor monitoring and control of the system. The water to be treated ispumped P-150 from the storage tanks into a first feed/blend tank T-100.A powdered sorbent or ion exchange material is loaded into a solidsfeeder which controls the rate of feed into the first feed/blend tankT-100.

The sorbent and the water are combined in a first feed/blend tank T-100and then in a second feed/blend tank T-101. Next, the treated water ispumped P-152 from the tanks to pass through a first solids removalfilter FLT-200 or a second solids removal filter FLT-201 (depending onwhich is online) to remove the sorbent and any other solids. Next thetreated water is pumped P-350 (of FIG. 6) through a first ultra filterFLT-300 or a second ultra filter FLT-301 (depending on which is online).

From the ultra filters the water is pumped P-450 through one or more ionspecific media (ISM) vessels containing ion exchange media specific tothe removal requirements of the site. In some embodiments the ISMvessels are loaded with a titanosilicate synthetic product, which is avery stable granular material with a high strontium distributioncoefficient Kd^(Sr), even in high competition (e.g., seawater, Ca andMg) making it an excellent choice for removal of strontium incolumn/vessel applications. The depicted embodiment shows four ISMvessels VSL-460, VSL-461, VSL-462, and VSL-463, three of which areonline and one which is in standby. After passing through one or more ofthe ISM vessels the water is either returned to the storage tanks or runthrough the system continuously until it meets purity standards. In someembodiments, the clean water may be used for system flushing operations.

FIGS. 7 through 16 depict the mechanical systems. Instrumentation andcontrol systems are described in FIGS. 17 through 24.

FIGS. 7 through 12 are detailed piping diagrams for the five exampleembodiment skids. In the depicted embodiments, every skid is equippedwith a sump into which fluid drains before recirculation or in whichwastes gather before disposal. In the depicted embodiments, each sumphas one or more drains, each preceded by a ball valve. The Control andSolids Feed skid 140 (FIG. 7) depicts one drain and one ball valve V-501(normally locked closed) located at a first end of the skid. TheFeed/Blend skid 130 (FIG. 8) sump has three drains, one at the first endwith ball valve V-121 (normally locked open), and two at the second endwith ball valves V-103 and V-122 (both normally locked closed). TheSolids Removal Filter skid 120 (FIG. 9) sump has three drains, two atthe first end with ball valves V-202 and V-217 (both normally lockedclosed), and one at the second end with ball valve V-218 (normallylocked closed). The Ultra Filter skid 110 (FIG. 10) sump has threedrains, two at the first end with ball valves V-301 and V-316 (bothnormally locked closed), and one at the second end with ball valve V-317(normally locked closed). The Ion Specific Media skid 100 (FIGS. 11-12)sump has three drains, one at the first end with ball valve V-412(normally locked closed), and two at the second end with ball valvesV-401 and V-413 (both normally locked closed).

FIG. 7 is a diagram depicting the mechanical components of an exampleembodiment Control and Solids Feed skid 140. The air in the Control andSolids Feed skid 140 is dehumidified by dryer DR-511. Air is passedthrough filter FLT-505 and passed through blower B-505. The blower B-505delivers the air at constant speed through a flex hose to the base of afirst hopper T-502. An in-line silencer S-504 may be placed after theblower B-505 to reduce noise. Alternative flow paths are provided whichmay be used, if necessary, to reduce air pressure in the system. Onesuch path vents to the room through a butterfly valve V-505 (normallyclosed) which is operated manually. The other path vents through apressure relief valve PRV-505 which will automatically release air whena maximum pressure is reached.

In an embodiment, powdered sorbents or ion exchange materials aredelivered in approximately 800 kg Super Sacks® or similar industrialsacks, hereinafter referred to as industrial sacks. The industrial sacksare unloaded through filter FLT-502 into the hopper T-502. Twomechanical vibrators VIB-503 and VIB-504 on either side of the hopperT-502 are used to aid the solid material in traveling to the base of thehopper T-502. At the base of the hopper T-502 a rotary valve RV-502controls the rate of flow of the solids through a flex coupling intosecond smaller hopper. The second hopper has a discharge at the inletwhich allows excess solids to flow out of the hopper in the event thehopper is overfilled. From the small hopper the solids travel into asolids feeder FDR-501 which uses an auger to control the feed rate ofthe solids. After the solids feeder FDR-501 stage, the sorbent is joinedby air and sent through a flex hose out of the Control and Solids Feedskid 140 to the Feed/Blend skid 130.

In an embodiment, the Feed/Blend skid 130, FIG. 8, has three inlets.Continuing with an embodiment depicted in FIG. 8, flush water may enterthe Feed/Blend skid 130 at a first inlet where it passes throughdisconnect valve DV-110. Flush water is usually used at system startupand to clean the pipes at system shutdown. Depending on which valve orvalves are open, the flush water may travel directly to one, two, orthree different locations in the skid. To deliver the flush water to thebeginning of the primary piping, ball valve V-102 (normally closed) maybe opened in which case the flush water will flow through ball valveV-102 and check valves CV-100 and CV-101. To deliver flush water to theprimary piping just before the first tank T-100, ball valve V-105(normally closed) may be opened in which case the flush water will flowthrough ball valve V-105 and check valves CV-105 and CV-109. Anotherflow path is provided to the sump if ball valve V-111 (normally lockedclosed) is opened. To deliver flush water to the secondary pipingbetween the outlets of the first and second tanks T-100 and T-101, ballvalve V-104 (normally closed) may be opened in which case the flushwater will travel through ball valve V-104 and checks valves CV-102 andCV-108. The ball valves may be fully opened or opened partially tocontrol the rate of flow. Depending on which valves are opened orclosed, the flush water can travel through any or all of the pipes inthe skid. Check valves are used to prevent flush water from flowing backto the source. Redundant check valves are used to increase the safetyfactor in the event pressure buildup compromises the first check valve.

At a second inlet RO reject water (or other nuclear process waste feedwater) is gravity fed into the system from the waste water storage tanksthrough double contained transfer hose H-001. The feed water is passedthrough a disconnect valve DV-100. Most or all of the feed water willcontinue through the primary piping, through ball valve V-106 (normallylocked open) and into a first feed/blend pump P-150, which is variablespeed. A portion of the feed water may travel through secondary pipingif ball valve V-108 (normally locked closed) is opened, and then travelthrough check valve CV-103 to bypass the first feed/blend pump P-150 andjoin the primary flow. The first feed/blend pump P-150 has twoadditional outlets with ball valves V-109 (normally closed) and V-107(normally locked closed) which direct excess water to the sump when oneor both valves are opened.

Water exits the first feed/blend pump P-150 where it passes throughcheck valve CV-104 and ball valve V-110 (normally locked open). The feedwater continues down the pipeline to a split where one path is normallyclosed and the other is open. On the normally open path, the feed waterpasses through ball valve V-123, is strained at basket strainer STR-100to remove particulates, and through ball valve V-124. If the normallyclosed path is opened, the feed water passes through ball valve V-125,basket strainer STR-101, and ball valve V-126. The normally open and thenormally closed paths converge prior to joining the powdered sorbent orion exchange material flow into the eductor ED-102. Three alternativepaths are provided for water flow to the sump which is blocked by valvesthat are normally locked closed. Ball valve V-128 controls flow on thealternative path from the normally closed primary line, ball valve V-129controls flow on the alternative path from the normally open primaryline, and ball valve V-127 controls flow on the alternative path justafter the convergence of the normally open and normally closed primarylines.

Continuing with an embodiment description, at a third inlet powderedsorbent or ion exchange material is provided from the Control and SolidsFeed skid 140 of FIG. 7 to the Feed/Blend Skid 130 of FIG. 8. Thepowdered sorbents or ion exchange materials travel through a flex hoseto eductor ED-102 where it joins the feed water. A motor operatedbutterfly valve MOV-102 serves as a vacuum break when delivery of thesorbent material is discontinued. This valve is normally closed duringoperation and fails in position. When the absorbent material flow isstopped, MOV-102 is opened to break the vacuum and prevent any furthermaterial from being drawn into the system. The movement of the feedwater in the eductor ED-102 creates a suction which draws the powderedsorbent or ion exchange materials into the first feed/blend tank T-100.The level in the first feed/blend tank T-100 will be automaticallycontrolled through modulation of the speed of first feed/blend pumpP-150. The level in the first feed/blend tank T-100 is controlled so theinlet feed flow will match the outlet flow. The powdered sorbent or ionexchange material dosing rate is set proportionately to the feed flowrate to maintain the proper ratio of sorbent powder to feed water. Themixed process water flows down through the first feed/blend tank T-100,out through ball valve V-112 (normally locked open) and flows into thesecond feed/blend tank T-101. An alternative path allows for bypass ofthe second feed/blend tank T-101 if ball valve V-101 (normally lockedclosed) is opened. Both tanks T-100 and T-101 have overflow runoff pathsat the top. The overflow is filtered through filters FLT-100 andFLT-101, passed through pressure relief valve PRV-101, which releasespressure when the pressure exceeds 0.10 MPA (15 PSIG), and proceeds tothe sump. The second feed/blend tank T-101 has a second alternative flowpath, which, if ball valve V-115 (normally locked closed) is opened,will allow for flow into the sump.

The process water leaves the second feed/blend tank T-101 through thebottom and through ball valve V-114 (normally locked open). Most or allof the process water will continue through the primary piping, throughball valve V-116 (normally locked open) and into a second feed/blendpump P-152, which is variable speed. The speed of the second feed/blendpump P-152 (FIG. 8) is modulated to maintain a constant pressure at theinlet to the ultra filter pump P-350 (FIG. 10). As the solids removalfilter is loaded, its differential pressure will increase and the speedof the second feed/blend pump P-152 (FIG. 8) will increase accordinglyto maintain a constant pressure downstream of the solids removal filter.By maintaining a constant pressure at the inlet to ultra filter pumpP-350 (FIG. 10), the flow through the solids removal filter must matchthe flow rate of ultra filter pump P-350 (FIG. 10). This also ensurespositive pressure is maintained on the suction side of ultra filter pumpP-350 (FIG. 10).

Continuing with the example embodiment of FIG. 8, a portion of theprocess water may travel through secondary piping if ball valve V-117(normally locked closed) is opened, and then travel through check valveCV-106 to bypass the second pump P-152 and rejoin the primary flowdownstream of the pump. The second feed/blend pump P-152 has twoadditional outlets with ball valves V-119 (normally closed) and V-118(normally locked closed) which direct excess water to the sump when oneor both valves are opened. The process water is then pumped throughdisconnect valve DV-101 and into double contained transfer hose H-002 tothe Solids Removal Filter skid 120.

In an example embodiment, the Solids Removal Filter skid 120, depictedin FIG. 9, has two inlets. At the first inlet, flush water may proceedthrough disconnect valve DV-206, ball valve V-201 (normally lockedclosed) and check valves CV-200 and CV-204. The flush water may travelalong any of the paths through the system depending on which valves areopen or closed.

Hydrogen and other gases may be vented from the filtering system justbefore each filter. The hydrogen or other gases may pass through ballvalve V-A (normally closed), through flex hose, through ball valve V-219(normally locked closed), and then either to the sump through ball valveV-200 (normally closed) or to the environment outside the skid throughfilter FLT-210. Alternatively, the hydrogen or other gases may travelthrough ball valve V-B (normally closed) and check valve CV-D to theenvironment. Nitrogen may be purged at either ball valve V-222 (normallylocked closed) or ball valve V-225 (normally locked closed) depending onwhich filter is currently in use.

At a second inlet, process water travels via double contained transferhose H-002 from the Feed/Blend skid 130 of FIG. 8. The process watertravels through disconnect valve DV-200. Most or all of the processwater will continue through the primary piping, through ball valve V-206(normally locked open) and check valve CV-201. Some of the process watermay flow to the sump if ball valve V-204 (normally closed) is opened. Ifball valve V-203 (normally locked closed) is opened, some, or all, ofthe process water may proceed into a solids removal filter pump P-250.Generally, solids removal filter pump P-250 will be bypassed.

If ball valve V-203 (normally locked closed) is opened, all or a portionof the process water will travel through secondary piping to the solidsremoval filter pump P-250. The solids removal filter pump P-250 has anadditional outlet with ball valve V-205 (normally closed) which allowsexcess process water to flow to the sump when it is opened.Additionally, just after the primary outlet, excess process water mayflow to the sump if ball valve V-226 (normally closed) is opened.However, most of the water will proceed through ball valve V-207(normally open) and check valve CV-202 back to the primary piping.

Along the primary pipeline, before the filters FLT-200 and FLT-201,there is a pressure relief valve PRV-200 which will relieve any pressureover 0.48 MPA (70 PSIG), or any pressure deemed crucial for propersystem operation. There is also a surge suppressor T-200 preceded byball valve V-216 (normally locked open) on a secondary line. Thepressure relief valve PRV-200 dumps process water to the sump when themaximum pressure is exceeded. The process water may either proceedthrough the first filter FLT-200 or the second filter FLT-201 dependingon which one is online. The filters FLT-200 and FLT-201 remove most ofthe contaminant-bearing powdered sorbent or ion exchange material andsmall particulates containing contaminants from the process water. Twofilters are provided with one online and one in standby or going througha replacement or maintenance procedure. The online filter remains onlineuntil the high differential pressure limit is reached. The standbyfilter is then placed online and the loaded filter can be replaced.

Continuing with an embodiment in FIG. 9, each filter FLT-200 and FLT-201is preceded by a disconnect valve DV-201 and DV-202, respectively, andfollowed by a disconnect valve DV-203 and DV-204, respectively, to allowfor simple removal and replacement. Disconnect valves DV-203 and DV-204are followed by ball valves V-214 (normally open) and V-215 (normallyopen), respectively. Alternatively, the filters FLT-200 and FLT-201 maybe bypassed entirely. If ball valves V-212 (normally locked closed) andV-213 (normally locked closed) are both opened, the process water canproceed along a secondary line through both valves and check valveCV-203 to the primary piping downstream of the filters FLT-200 andFLT-201. After the filters FLT-200 and FLT-201, if ball valve V-209(normally closed) is open, some of the process water may proceed to thesump. Generally, the process water will proceed through disconnect valveDV-205 into flex hose H-003 for transport to the Ultra Filter skid 110(FIG. 10).

In an embodiment, the Ultra Filter skid 110, FIG. 10, operates much likethe Solids Removal Filter skid 120 (FIG. 9) except that the pump is onthe primary line instead of a secondary line. As mentioned previously,the speed of the ultra filter feed pump P-350 will be modulated tomaintain a constant flow through the ultra filters FLT-300 and FLT-301using a magnetic flow meter. As the filter is loaded and thetrans-membrane pressure increases, the ultra filter feed pump P-350speed will increase in order to maintain the flow rate set point. Ultrafilter pump P-350 will be sized to ensure positive pressure ismaintained at the inlet to the ISM feed pump P-450 of FIG. 11.

In an embodiment, the Ultra Filter skid 110 as shown in FIG. 10, has twoinlets. At the first inlet, flush water may proceed through disconnectvalve DV-306, ball valve V-302 (normally locked closed), and checkvalves CV-300 and CV-303. The flush water may travel along any of thepaths through the system depending on which valves are open or closed.

Hydrogen and other gases may be vented from the filtering system justafter each filter placement in the process line. The hydrogen or othergases may pass through ball valve V-A (normally closed), through flexhose, through ball valve V-315 (normally closed), and then either to thesump through ball valve V-300 (normally closed) or to the environmentoutside the skid through filter FLT-310. Alternatively, the hydrogen orother gases may travel through ball valve V-B (normally closed) andcheck valve CV-D to the environment. Nitrogen may be purged at eitherball valve V-320 (normally closed) or ball valve V-323 (normally closed)depending on which filter is currently in use.

At a second inlet, process water travels via double contained transferhose H-003 from the Solids Removal Filter skid 120 of FIG. 9. Continuingwith an embodiment of FIG. 10, the process water travels throughdisconnect valve DV-300 and through ball valve V-303 (normally lockedopen) to the ultra filter pump P-350. The ultra filter pump P-350 has anadditional outlet with ball valve V-305 (normally closed) which allowsexcess process water to flow to the sump when it is opened.Additionally, just after the primary outlet, excess process water mayflow to the sump if ball valves V-326 (normally closed) and V-304(normally closed) are opened. If ball valve V-304 (normally closed) isopened, process water may bypass the pump and travel to the sump.However, most of the water will proceed through ball valve V-306(normally locked open) and check valve CV-301 back to the primarypiping.

Along the primary pipeline, before the filters FLT-300 and FLT-301,there is a pressure relief valve PRV-300 which will relieve any pressureover 1.03 MPA (150 PSIG), or any pressure deemed crucial for propersystem operation. There is also a surge suppressor T-300 preceded byball valve V-307 (normally locked open) on a secondary line. Thepressure relief valve PRV-300 dumps process water to the sump when thepressure is exceeded. The process water may either proceed through thefirst filter FLT-300 or the second filter FLT-301 depending on which oneis online. The filters FLT-300 and FLT-301 remove most of the remainingcontaminant bearing solids and small particulate containing contaminantsfrom the process water. Two filters are provided with one online and onein standby or being replaced. The online filter remains online until thehigh differential pressure limit is reached. The standby filter is thenplaced online and the loaded filter can be replaced.

Further with an embodiment of FIG. 10, each of the filters FLT-300 andFLT-301 are preceded by a disconnect valve DV-301 and DV-302,respectively, and followed by a disconnect valve DV-303 and DV-304,respectively, to allow for simple removal and replacement. Disconnectvalves DV-303 and DV-304 are followed by ball valves V-313 (normallyopen) and V-314 (normally open), respectively. Alternatively, thefilters FLT-300 and FLT-301 may be bypassed entirely. If ball valvesV-311 (normally locked closed) and V-312 (normally locked closed) areboth opened, the process water can proceed along a secondary linethrough both valves and check valve CV-302 to the primary piping at theother side of the filters FLT-300 and FLT-301. After the filters FLT-300and FLT-301, if ball valve V-309 (normally closed) is open, some of thefiltered process water may proceed to the sump. Generally, the filteredprocess water will proceed through disconnect valve DV-305 into flexhose 1H-004 for transport to the Ion Specific Media skid 100 of FIG. 11.

The Ion Specific Media skid 100, depicted in an embodiment in FIGS. 11and 12, has two inlets. In an embodiment, at the first inlet, flushwater may proceed through disconnect valve DV-410, ball valve V-402(normally locked closed), and check valves CV-400 and CV-402. The flushwater may travel along any of the paths through the system depending onwhich valves are open or closed.

At a second inlet, filtered process water travels via double containedtransfer hose H-004 from the Ultra Filter skid 110 of FIG. 10. Thefiltered process water travels through disconnect valve DV-400 andthrough ball valve V-403 (normally locked open) to the ISM feed pumpP-450. If ball valve V-404 (normally closed) is opened, filtered processwater may travel to the sump. The pump P-450 has an additional outletwith ball valve V-405 (normally closed) which allows excess filteredprocess water to flow to the sump when it is opened. Additionally, justafter the primary outlet, excess filtered process water may flow to thesump if ball valve V-415 (normally closed) is opened. Generally, thefiltered process water will proceed through check valve CV-401 and ballvalve V-406 (normally locked open) back to the primary piping.

The ISM feed pump P-450 is a constant speed pump, with variable speedcapability, sized for transfer through the ISM vessels and for return tothe storage tanks. The speed of the ISM feed pump P-450 will be adjustedmanually from the control system to ensure sufficient head is availablefor the transfer function. Variable speed capability allows forflexibility of operation in different modes or for different transferlengths. The pressure differential through the ISM vessels and back tothe feed tanks does not generally change significantly, thereforesetting the ISM feed pump P-450 at a constant speed reduces thecomplexity of the control system. Sufficient pressure and flowinstrumentation is included to provide proportional feedback control onthe ISM feed pump P-450, if desired based on operating experience.

Along the primary pipeline, before the ISM vessels, there is a pressurerelief valve PRV-400 which will relieve any pressure over 0.90 MPA (130PSIG), or any pressure deemed crucial for proper system operation. Thereis also a surge suppressor T-400 on a secondary line. The pressurerelief valve PRV-300 dumps filtered process water to the sump when thepressure is exceeded. The filtered process water proceeds to the ISMvessels (FIG. 12). Two points in the ISM vessel pipe configuration allowfor excess filtered process water to flow to the sump if ball valveV-409 (normally closed) and/or ball valve V-410 (normally closed) areopen. After the filtered process water has gone through the ISM vesselsit flows through a disconnect valve DV-409 through flex hose HI-005 backto the storage tanks.

In an embodiment, FIG. 12 depicts the ISM vessels on the Ion SpecificMedia skid 100 of FIG. 11. Generally, three of the four ISM vessels areonline at one time and the fourth column is in standby or beingexchanged with a fresh vessel. The standby ISM vessel is selected fromthe control system and the motor operated valves are automaticallyaligned. In one embodiment, the system is operated with three ISMvessels on line at one time (alternative day/time on line configurationsmay be used based on media used, conditions to be treated, and systemdesign), after which the next ISM vessel in sequence is selected as thestandby ISM vessel. The standby ISM vessel is then replaced with a freshISM vessel. In the depicted embodiment ISM vessel VSL-463 is in standby.The length of time each ISM vessel is in use is dependent on theparticular ISM used and the targeted isotope to be removed.

Continuing with an embodiment of FIG. 12, each ISM vessel (four tanksdenoted in FIG. 12 as VSL-xxx) is connected to the pipes with disconnectvalves for quick removal and replacement. ISM vessel VSL-460 isconnected with disconnect valves DV-401 and DV-402. ISM vessel VSL-461is connected with disconnect valves DV-403 and DV-404. ISM vesselVSL-462 is connected with disconnect valves DV-405 and DV-406. ISMvessel VSL-463 is connected with disconnect valves DV-407 and DV-408.Each vessel is connected to ball valve V-Z (normally closed), ball valveV-Y (normally closed) followed by check valve CV-Y, and ball valve V-X(normally closed) followed by a drain.

Filtered process water is pumped into the ISM vessel system from ISMfeed pump P-450. The filtered process water flows into each ISM vessel.After each ISM vessel the filtered process water flows either to thenext ISM vessel or out of the ISM vessel system to FIG. 11. The flowthrough the ISM vessel system is heavily controlled with motor operatedball valves (depicted in FIG. 24).

FIGS. 13 through 16 are piping diagrams for example embodiment depictingSample Enclosures for each of the skids.

FIG. 13 is a diagram depicting the mechanical components in an exampleembodiment Sample Enclosure for an example embodiment Feed/Blend skid.In the embodiment, a first sample is taken downstream from the firstfeed/blend pump P-150 (of FIG. 8). The sample is sent through gate valveV-130 and through the sample valve assembly MVD-100. A portion of thesample is directed to sample port S-100 then through check valve CV-130and finally out to the sump. The remainder of the sample is sent to agate valve V-131, a check valve CV-131 and then returned to the primarypiping just upstream of the second feed/blend tank T-101 (of FIG. 8). Asecond sample is taken downstream from the second feed/blend pump P-152(of FIG. 8). Continuing with an embodiment of FIG. 13, the sample issent through gate valve V-132 and through the sample valve assemblyMVD-101. A portion of the sample is directed to sample port S-101 thenthrough check valve CV-132 and finally out to the sump. The remainder ofthe sample is sent to a gate valve V-133, a check valve CV-133 and thenreturned to the primary piping just before the second feed/blend tankT-101.

FIG. 14 is a diagram depicting the mechanical components in an exampleembodiment Sample Enclosure for an example embodiment Solids RemovalFilter skid 120. A first sample is taken downstream of the SolidsRemoval Filter pump P-250 (of FIG. 9) before the filters FLT-200 andFLT-201 (both of FIG. 9). Continuing with an embodiment of FIG. 14, thesample is sent through gate valve V-230 and through the sample valveassembly MVD-200. A portion of the sample is directed to sample portS-200 then through check valve CV-230 and finally out to the sump. Theremainder of the sample is sent to a gate valve V-231, a check valveCV-231 and then returned to the primary piping at the second end of theskid (depicted in an embodiment of FIG. 9). A second sample is takenjust after the filters FLT-200 and FLT-201 (of FIG. 9). The sample issent through gate valve V-232 and through the sample valve assemblyMVD-201. A portion of the sample is directed to sample port S-201 thenthrough check valve CV-232 and finally out to the sump. The remainder ofthe sample is sent to a gate valve V-233, a check valve CV-233 and thenreturned to the primary piping at the second end of the skid (depictedin an embodiment of FIG. 9).

FIG. 15 is a diagram depicting the mechanical components in an exampleembodiment Sample Enclosure for an example embodiment Ultra Filter skid110. A first sample is taken downstream of the ultra filter pump P-350before the filters FLT-300 and FLT-301 (of FIG. 10). The sample is sentthrough gate valve V-330 and through the sample valve assembly MVD-300.A portion of the sample is directed to sample port S-300 then throughcheck valve CV-330 and finally out to the sump. The remainder of thesample is sent to a gate valve V-331, a check valve CV-331 and thenreturned to the primary piping at the second end of the skid (depictedin an embodiment of FIG. 10). A second sample is taken just downstreamof the filters FLT-300 and FLT-301 (of FIG. 10). The sample is sentthrough gate valve V-332 and through the sample valve assembly MVD-301.A portion of the sample is directed to sample port S-301 then throughcheck valve CV-332 and finally out to the sump. The remainder of thesample is sent to a gate valve V-333, a check valve CV-333 and thenreturned to the primary piping at the second end of the skid (depictedin FIG. 10).

FIG. 16 is an example embodiment piping diagram for the Sample Enclosurefor the Ion Specific Media skid 100. A sample is taken just beforeentering the ISM vessel assembly of FIG. 12. This sample is sent throughgate valve V-438 and through the sample valve assembly MVD-400. Aportion of the sample is directed to sample port S-400 then throughcheck valve CV-438 and finally out to the sump. The remainder of thesample is sent to a gate valve V-439, a check valve CV-439 and thenreturned to the primary piping at the first end of the skid (depicted inFIG. 11). Additional samples are taken just downstream of each ISMvessel (depicted in FIG. 12).

Continuing with an embodiment of FIG. 16, the sample from ISM vesselVSL-460 (of FIG. 12) is sent through gate valve V-430 to sample valveassembly MVD-460. A portion of the sample is directed to sample portS-460 then through check valve CV-430 and finally out to the sump. Theremainder of the sample is sent to a gate valve V-431, a check valveCV-431 and then returned to the primary piping at the first end of theskid (depicted in FIG. 11). The sample from ISM vessel VSL-461 (of FIG.12) is sent through gate valve V-432 to sample valve assembly MVD-461. Aportion of the sample is directed to sample port S-461 then throughcheck valve CV-432 and finally out to the sump. The remainder of thesample is sent to a gate valve V-433, a check valve CV-433 and thenreturned to the primary piping at the first end of the skid (depicted inFIG. 11). The sample from ISM vessel VSL-462 (of FIG. 12) is sentthrough gate valve V-434 to sample valve assembly MVD-462. A portion ofthe sample is directed to sample port S-462 then through check valveCV-434 and finally out to the sump. The remainder of the sample is sentto a gate valve V-435, a check valve CV-435 and then returned to theprimary piping at the first end of the skid (depicted in FIG. 11). Thesample from ISM vessel VSL-463 is sent through gate valve V-436 tosample valve assembly MVD-463. A portion of the sample is directed tosample port S-463 then through check valve CV-436 and finally out to thesump. The remainder of the sample is sent to a gate valve V-437, a checkvalve CV-437 and then returned to the primary piping at the first end ofthe skid (depicted in FIG. 11).

Controls/Instrumentation

In an embodiment, the Control and Solids Feed skid 140 (FIGS. 7 and 19)houses the control system. This system utilizes an Allen-Bradley, orcomparable, Compact Logix Programmable Logic Controller (PLC) to provideprocess logic for the entire system. The touchscreen HMI mounted to theface of the control panel provides access to the entire control system.However, the advanced logic allows a very simple start and stop to theprocess. This system provides both the local interface for monitoringand control operations at the control skid and also a remote controlroom interface for monitoring only. In addition to skid operationalcontrols and interlocks, the control system provides data recording andreporting, radiation detection monitoring, and video camera monitoringfor each skid. Operational space for the controls require one half ofthe available space of the physical skid. The other half houses thesolids feed system as depicted in FIG. 7. In the depicted embodiment,the Control Skid is combined with the Solids Feed Skid to form theControl and Solids Feed Skid 140. In some embodiments, the Control Skidand the Solids Feed Skid are separate. Control may occur entirely onsite, remotely, or both. On-site control may occur entirely within aControl Skid, within a combined Control and Solids Feed Skid 140, or itmay be augmented with either remote control from a remotely locatedcontrol station or from mobile devices such as smart phones, tablets,and laptop computers.

General Instrumentation

FIG. 17 depicts a typical gauge valve and pressure differentialindicating transmitter (PDIT) manifold.

FIG. 18 is a legend describing instrumentation symbols. Instrumentinterlocks are used to prevent operators and/or machinery from beingharmed in the event of a leak or other failure. Interlock 1 I1 shutsdown all pumps on leak detection, interlock 2 I2 shuts down pumps onhigh level, interlock 3 I3 shuts down pumps on low level, and interlockI4 de-energizes the associated valve on leak detection. Circles indicatefield-mounted instruments and circles within squares indicate computerdialog or control elements. A dashed line indicates an electrical orcontrol signal. Each instrument is labeled with a two or three digitabbreviation and a three digit number. The abbreviations used are listedin the figure.

FIGS. 19 through 24 show example instrumentation for the five exampleskids.

Sump Instrumentation

In an embodiment, every skid has a sump and every sump has at least oneleak detection transmitter which transmits to a leak detection alarm inthe event a leak is detected. Each leak detection data line has at leastone interlock. In an embodiment, the Control and Solids Feed skid 140(FIG. 19) has one leak detection transmitter LDT-500 which is connectedto leak detection alarm LDA-500 equipped with interlock I1. TheFeed/Blend skid 130 (FIG. 20) has two leak detection transmittersLDT-100 and LDT-101 which are connected to leak detection alarms LDA-100and LDA-101, respectively, both equipped with interlocks I1 and I4. Inan embodiment, the Solids Removal Filter skid 120 (FIG. 21) has two leakdetection transmitters LDT-200 and LDT-201 which are connected to leakdetection alarms LDA-200 and LDA-201, respectively, both equipped withinterlocks I1 and I4. The Ultra Filter skid 110 (FIG. 22) has two leakdetection transmitters LDT-300 and LDT-301 which are connected to leakdetection alarms LDA-300 and LDA-301, respectively, both equipped withinterlocks I1 and I4. The Ion Specific Media skid 100 (FIGS. 23-24) hastwo leak detection transmitters LDT-400 and LDT-401 which are connectedto leak detection alarms LDA-400 and LDA-401, respectively, bothequipped with interlocks I1 and I4.

Environmental Monitoring Instrumentation

In an embodiment, every skid is also equipped with at least onetemperature transmitter and at least one radiation detectiontransmitter. The Control and Solids Feed skid 140 (FIG. 19) uses atemperature transmitter TT-502 in the solids loading room to transmitthe ambient temperature to a hand indicator HI-502, moisture indicatorMI-502, and temperature indicator TI-502. A radiation detectiontransmitter RDT-510 is used in the control room to transmit radiationlevels to a radiation indicator RI-510. The Feed/Blend skid 130 (FIG.20) has a temperature transmitter TT-102 that transmits ambient skidtemperature data to temperature indicator TI-102 and moisture indicatorMI-102. Radiation levels are monitored by radiation detectiontransmitter RDT-110 and transmitted to radiation indicator RI-110.

In an embodiment, the Solids Removal Filter skid 120 (FIG. 21) has atemperature transmitter TT-202 that transmits ambient skid temperaturedata to temperature indicator TI-202 and moisture indicator MI-202. Skidradiation levels are monitored by radiation detection transmitterRDT-210 and transmitted to radiation indicator RI-210. Additionally,radiation levels are monitored by radiation detection transmittersRDT-200 and RDT-201 which are placed in proximity to filters FLT-200 andFLT-201, respectively. Radiations levels are transmitted to radiationindicators RI-200 and RI-201, respectively.

In an embodiment, the Ultra Filter skid 110 (FIG. 22) has a temperaturetransmitter TT-302 that transmits ambient skid temperature data totemperature indicator TI-302 and moisture indicator MI-302. Skidradiation levels are monitored by radiation detection transmitterRDT-310 and transmitted to radiation indicator RI-310. Additionally,radiation levels are monitored by radiation detection transmittersRDT-300 and RDT-301 which are placed in proximity to filters FLT-300 andFLT-301, respectively. Radiations levels are transmitted to radiationindicators R-300 and R-301, respectively.

In an embodiment, ambient skid temperature for the Ion Specific Mediaskid 100 (FIGS. 23-24) is sensed by temperature transmitter TT-402 andsent to moisture indicator MI-402 and temperature indicator TI-402. Aradiation detecting transmitter RDT-460, RDT-461, RDT-462, and RDT-463is placed in proximity to each ISM vessel. Each radiation detectingtransmitter is connected to a corresponding radiation indicator R-460,R-461, RI-462, and R-463.

Flow Controls

In an embodiment, all of the skids except the Control and Solids Feedskid 140 (FIG. 19) have motor operated ball valves for regulating flowinto and out of the skid, as well as within the skid.

In an embodiment, the Feed/Blend skid 130 (FIG. 20) has motor operatedball valve MOV-100 (fails closed), equipped with interlock I4, at thefirst end of the skid at the water feed point controlled by eventcontroller YC-100. Flow out of the skid is regulated by motor operatedball valve MOV-101 (fails as-is) which is controlled by event controllerYC-101. A motor operated butterfly valve MOV-102 serves as a vacuumbreak when delivery of the sorbent material is discontinued. This valveis normally closed during operation and fails in position. When theabsorbent material flow is stopped, MOV-102 is opened to break thevacuum and prevent any further material from being drawn into thesystem. MOV-102 is controlled by event controller YC-102.

In an embodiment, the Solids Removal Filter skid 120 (FIG. 21) has motoroperated ball valve MOV-200 (fails as-is), controlled by eventcontroller YC-200, at the inlet of the skid to regulate incoming flowfrom the Feed/Blend skid 130 (FIG. 20). Flow out of the skid isregulated by motor operated ball valve MOV-203 (fails as-is) which iscontrolled by event controller YC-203. Motor operated ball valvesMOV-201 and MOV-202 (both fail as-is) are used to regulate the flowbefore each filter FLT-200 and FLT-201, respectively. Motor operatedball valves MOV-201 and MOV-202 are controlled by event controllersYC-201 and YC-202, respectively.

In an embodiment, the Ultra Filter skid 110 (FIG. 22) has motor operatedball valve MOV-300 (fails as-is), controlled by event controller YC-300,at the inlet of the skid to regulate incoming flow from the SolidsRemoval Filter skid (FIG. 21). Flow out of the skid is regulated bymotor operated ball valve MOV-303 (fails as-is) which is controlled byevent controller YC-303. Motor operated ball valves MOV-301 and MOV-302(both fail as-is) are used to regulate the flow before each filterFLT-300 and FLT-301, respectively. Motor operated ball valves MOV-301and MOV-302 are controlled by event controllers YC-301 and YC-302,respectively.

In an embodiment, the Ion Specific Media skid (FIGS. 23-24) has motoroperated ball valve MOV-400 (fails as-is), controlled by eventcontroller YC-400, at the inlet of the skid to regulate incoming flowfrom the Ultra Filter skid (FIG. 22). Motor operated ball valves MOV-401through MOV-421 (all fail as-is) are positioned throughout the ISMvessel system as shown. Each motor operated ball valve is controlledwith an event controller YC-401 through YC-421 where the motor operatedball valve and event controller share identification numbers. Motoroperated ball valve MOV-422 (fails as-is), controlled by eventcontroller YC-422, is used to regulate flow leaving the skid.

In an embodiment, downstream from the first pump on each skid a magneticflow meter is used to monitor flow out of the pump. In the Feed Blendskid 130 (FIG. 20) the magnetic flow meter is connected to a flowindicating transmitter FIT-100 which is further connected to a flowindicator FI-100. In the Solids Removal Filter skid 120 (FIG. 21) themagnetic flow meter is connected to a flow indicating transmitterFIT-200 which is further connected to a flow indicator FI-200. In theUltra Filter skid 110 (FIG. 22) the magnetic flow meter is connected toa flow indicating transmitter FIT-350 which is further connected to aflow indicator FI-350. In the Ion Specific Media skid 100 (FIGS. 23-24)the magnetic flow meter is connected to a flow indicating transmitterFIT-400 which is further connected to a flow indicator FI-400, which isconnected via data link to speed controller SC-450.

Pressure Indicators and Controls

In an embodiment, pressure is monitored at critical points in all of theskids.

In the Feed/Blend skid 130 (FIG. 20) the pressure in the feed/blendtanks T-100 and T-101 is monitored by pressure indicating transmittersPIT-102 and PIT-106, respectively. PIT-102 and PIT-106 are connected topressure indicators PI-102 and PI-106, respectively. Pressure ismonitored just before the eductor ED-102 at both inputs with pressureindicating transmitters PIT-108 and PIT-109 which are connected topressure indicators PI-108 and PI-109, respectively. Pressure ismonitored upstream and downstream of the first feed/blend pump P-150 bypressure indicating transmitters PIT-100 and PIT-101 which are connectedto pressure indicators PI-100 and PI-101, respectively. Pressure ismonitored upstream and downstream of the second feed/blend pump P-152 bypressure indicating transmitters PIT-104 and PIT-105, both connected todiaphragms, which are connected to pressure indicators PI-104 andPI-105, respectively.

In the Solids Removal Filter skid 120 (FIG. 21) the pressure upstream ofthe solids removal filter pump P-250 is monitored by pressure indicatingtransmitter PIT-200, connected to gauge valve GV-200. PIT-200 isconnected to pressure indicator PI-200. Pressure is monitored bothupstream and downstream of the filters by pressure indicatingtransmitters PIT-201, connected to a diaphragm, and PIT-202, connectedto gauge valve GV-202. PIT-201 and PIT-202 are connected to pressureindicators PI-201 and PI-202, respectively. PI-201 and PI-202 are bothconnected via data link to pressure differential indicator PDI-200.Additionally, pressure is monitored at the surge suppressor by pressureindicator PI-207.

In the Ultra Filter skid 110 (FIG. 22) pressure is monitored just beforethe ultra filter pump P-350 using pressure indicating transmitterPIT-300, connected to gauge valve GV-300. PIT-300 is connected topressure indicating controller PIC-300 which is further connected bydata link to the second feed/blend pump P-152 (FIG. 20) controls.Pressure is monitored both upstream and downstream of the filters bypressure indicating transmitters PIT-301, connected to gauge valveGV-301, and PIT-302, connected to gauge valve GV-302. PIT-301 andPIT-302 are connected to pressure indicators PI-301 and PI-302,respectively. PI-301 and PI-302 are both connected via data link topressure differential indicator PDI-300. Additionally, pressure ismonitored at the surge suppressor by pressure indicator PI-307.

In the Ion Specific Media skid 100 (FIGS. 23-24) pressure is indicatedboth before and after the ISM feed pump P-450. Before the ISM feed pumpP-450, pressure indicating transmitter PIT-400, connected to gauge valveGV-400 is connected to pressure indicating controller PIC-400 which isconnected via a data link to ultra filter feed pump P-350 controls.After the ISM feed pump P-450, pressure indicating transmitter PIT-401connected to gauge valve GV-401, is connected to pressure indicatorPI-401. A pressure indicator PI-407 is connected to surge suppressorT-400. Four pressure differential indicating transmitters PDIT-400,PDIT-401, PDIT-402, and PDIT-403 are situated between the inlet andoutlet of each ISM vessel. PDIT-400, PDIT-401, PDIT-402, and PDIT-403are connected to pressure differential indicators PDI-400, PDI-401,PDI-402, and PDI-403, respectively. A pressure indicating transmitterPIT-402 is located just before motor operated ball valve MOV-422 and isconnected to a pressure indicator PI-402.

Pump Controls

In an embodiment, the Feed/Blend skid 130 (FIG. 20) has two pumps. Thefirst feed/blend pump P-150 is connected to variable frequency driveVFD-150, equipped with interlocks I1 and I2. Variable frequency driveVFD-150 is connected to event controllers YC-150A and YC-150B, eventindicators YI-150A and YI-150B, and speed controller SC-150. The firstfeed/blend pump P-150 controls are connected via data link to the levelcontrols of the first feed/blend tank T-100. The level in the firstfeed/blend tank T-100 will be automatically controlled throughmodulation of the speed of the first feed/blend pump P-150. The level inthe first feed/blend tank T-100 is controlled so the inlet feed flowwill match the outlet flow.

The second feed/blend pump P-152 is connected to variable frequencydrive VFD-152, equipped with interlocks I1 and I3. Variable frequencydrive VFD-152 is connected to event controllers YC-152A and YC-152B,event indicators YI-152A and YI-152B, and speed controller SC-152. Thesecond feed/blend pump P-152 controls are connected via data link to thepressure indicating controller PIC-300 (FIG. 22) that indicates andcontrols pressure just upstream of the ultra filter pump P-350 (FIG.22).

In an embodiment, the speed of the second feed/blend pump P-152 ismodulated to maintain a constant pressure at the inlet to the ultrafilter pump P-350 (FIG. 22). As the solids removal filter is loaded, itsdifferential pressure will increase and the speed of the secondfeed/blend pump P-152 will increase accordingly to maintain a constantpressure downstream of the solids removal filter. By maintaining aconstant pressure at the inlet to ultra filter pump P-350 (FIG. 22), theflow through the solids removal filter must match the flow rate of ultrafilter pump P-350 (FIG. 22). This also ensures positive pressure ismaintained on the suction side of ultra filter pump P-350 (FIG. 22).

In an embodiment, within the Solids Removal Filter skid 120 (FIG. 21)the solids removal filter pump P-250 will generally be bypassed. Solidsremoval filter pump P-250 is connected to variable frequency driveVFD-250, equipped with interlock I1. Variable frequency drive VFD-250 isconnected to event controllers YC-250A and YC-250B, event indicatorsYI-250A and YI-250B, and speed controller SC-250.

In an embodiment, the Ultra Filter skid 110 (FIG. 22) the ultra filterpump P-350 is connected to variable frequency drive VFD-350, equippedwith interlock I1. Variable frequency drive VFD-350 is connected toevent controllers YC-350A and YC-350B, event indicators YI-350A andYI-350B, and speed controller SC-350. The ultra filter pump controlsP-350 are connected via data link to the pressure indicating controllerPIC-400 (FIG. 23) that indicates and controls pressure just upstream ofthe ISM feed pump P-450 (FIG. 23). The speed of the ultra filter pumpP-350 will be modulated to maintain a constant flow through the ultrafilters FLT-300 and FLT-301 using a magnetic flow meter. As the filteris loaded and the trans-membrane pressure increases, the ultra filterpump P-350 speed will increase in order to maintain the flow rate setpoint. Ultra filter pump P-350 will be sized to ensure positive pressureis maintained at the inlet to the ISM feed pump P-450 (FIG. 23).

In an embodiment, within the Ion Specific Media skid 100 (FIGS. 23-24)the ISM feed pump P-450 is connected to variable frequency driveVFD-450, equipped with interlock I1. Variable frequency drive VFD-450 isconnected to event controllers YC-450A and YC-450B, event indicatorsYI-450A and YI-450B, and speed controller SC-450. The ISM feed pumpP-450 is a constant speed pump, with variable speed capability, sizedfor transfer through the ISM vessels and for return to the storagetanks. The speed of the ISM feed pump P-450 will be adjusted manuallyfrom the control system to ensure sufficient head is available for thetransfer duty. Variable speed capability allows for flexibility ofoperation in different modes or for different transfer lengths. Thepressure differential through the ISM vessels and back to the feed tanksdoes not generally change significantly, therefore setting this pump ata constant speed reduces the complexity of the control system.Sufficient pressure and flow instrumentation is included to provideproportional feedback control on ISM feed pump P-450, if desired basedon operating experience.

Other Instrumentation

FIG. 19 is a diagram depicting instrumentation of an example embodimentControl and Solids Feed skid 140. The ventilation system is monitoredand controlled by a moisture indicator/controller MIC-511. The blowerB-505 is controlled by event controller YC-505. The mass of the powderedsorbent or ion exchange material in the solids feeder FDR-501 ismonitored by weight transmitter WT-501 and indicated by weight indicatorWI-501. A level switch low LSL-502 is used in the hopper T-502 totransmit the status to a level alarm indicator LAL-502 when the amountof sorbent in the hopper T-502 is too low. Event controllers YC-503 andYC-504 are used to control the mechanical vibrators VIB-503 and VIB-504,respectively. Event controller YC-506 is used to control the rate offeed of the sorbent through a motor operated butterfly valve MOV-506into the hopper T-502. Event controller YC-502 is used to control themotorized rotary valve RV-502 between the hopper T-502 and the solidsfeeder FDR-501 to regulate the rate of feed of the sorbent. Speedcontroller SC-501 and event controller YC-501 control the rate of thesolids feeder FDR-501.

FIG. 20 is a diagram depicting instrumentation of an example embodimentFeed/Blend skid 130. Both feed/blend tanks are monitored for fill level.Each of the feed/blend tanks T-100 and T-101 has a level switch highLSH-100 and LSH-101 (respectively), equipped with interlock I2, and alevel switch low LSL-100 and LSL-101 (respectively), equipped withinterlock I3. Level switches high LSH-100 and LSH-101 are connected tolevel alarms high LAH-100 and LAH-101, respectively. Likewise, levelswitches low LSL-100 and LSL-101 are connected to level alarms lowLAL-100 and LAL-101, respectively. Level switches indicate when the tankis too full or too low.

The level in each of the feed/blend tanks T-100 and T-101 is monitoredby a pressure indicating transmitter PIT-103 and PIT-107 (respectively),each connected to a diaphragm. PIT-103 is connected to level switchindicator LSI-103, level switch high LSH-103, and level indicatingcontroller LIC-103. LIC-103 is further connected to the first feed/blendpump P-150 controls. PIT-107 is connected to level indicator LI-107.

Downstream of the magnetic flow meter pH and turbidity are monitored byanalyzer sensor AE-100, conductivity sensor CE-100, and analyzer sensorAE-101. Analyzer sensor AE-100 and conductivity sensor CE-100 areconnected to conductivity transmitter CT-100 which is connected toanalyzer indicator AI-100, temperature indicator TI-100, andconductivity indicator CI-100. Analyzer sensor AE-101 is connected toanalyzer transmitter AT-101 which is connected to analyzer indicatorAI-101.

FIG. 21 is a diagram depicting instrumentation of an example embodimentSolids Removal Filter skid 120. Conductivity is monitored before andafter the filters with conductivity sensor CE-200 and conductivitytransmitter CT-200 before the filters and conductivity sensor CE-201after the filters. Conductivity sensor CE-200 and conductivitytransmitter CT-200 are connected to conductivity indicator CI-200 andtemperature indicator TI-200. Conductivity sensor CE-201 is connected toconductivity transmitter CT-200 which is connected to conductivityindicator CI-201 and temperature indicator TI-201. A leak detectiontransmitter LDT-202 is located on the gas purge line. When a leak isdetected a local light is activated to indicate the leak. Turbidity ismonitored at the second end of the skid. Analyzer sensor AE-200 isconnected analyzer transmitter AT-200 which is connected analyzerindicator AI-200.

FIG. 22 is a diagram depicting instrumentation of an example embodimentUltra Filter skid 110. Conductivity is monitored before and after thefilters with conductivity sensor CE-300 and conductivity transmitterCT-300 before the filters and conductivity sensor CE-301 andconductivity transmitter CT-301 after the filters. Conductivity sensorCE-300 and conductivity transmitter CT-300 are connected to conductivityindicator CI-300 and temperature indicator TI-300. Conductivity sensorCE-301 and conductivity transmitter CT-301 after the filters areconnected to conductivity indicator CI-301 and temperature indicatorTI-301. A leak detection transmitter LDT-302 is located on the gas purgeline. When a leak is detected a local light is activated to indicate theleak.

FIGS. 23 and 24 are diagrams depicting instrumentation of an exampleembodiment Ion Specific Media skid 100. Just after the motor-operatedball valve MOV-400 a conductivity sensor CE-400 is connected to aconductivity transmitter CT-400 which is then connected to aconductivity indicator CI-400 and a temperature indicator TI-400.Additionally, the conductivity transmitter CT-400 is connected to aconductivity sensor CE-401 in the ISM vessel system and transmits theconductivity data to a conductivity indicator CI-401 and a temperatureindicator TI-401.

Startup/Nominal Values

In an embodiment of a startup procedure, the piping system will befilled and vented by clean water injected through the flush connections.RO reject feed flow is started with second feed/blend pump P-152 and thepowdered sorbent or ion exchange material feed is initiated. The firstfeed/blend tank T-100 is allowed to fill to its normal operating level.When the tank reaches the high level, the downstream pumps P-152, P-350,and P-450 are started in sequence. Second feed/blend pump P-152 isstarted initially with a permissive from a second feed/blend tank T-101level set point and positive pressure at its suction. Ultra filter pumpP-350 will then start when its suction pressure reaches a positive valuethrough a permissive on its suction side pressure transmitter. ISM feedpump P-450 will then start when its suction pressure reaches a positivevalue through a permissive on its suction side pressure transmitter.Variable speed drives will be set for slow pump ramp up to a fixedspeed. Once all pumps are up to speed, the system is transferred toautomatic control and the normal operation sequence described abovetakes over.

Optimal System Operation

With consideration now for the projected number of filters and ISMvessels to be generated in the spent SRF, UF, and ISM vessels. Thenumber of SRFs generated is related to how much powdered sorbent or ionexchange material is used. The baseline operation is to use 400 kgsorbent per 1,000 m³ of water with the expectation of generating fivespent SRFs per 5,000 m³ of water. The sorbent usage could be as low 100kg per 1,000 m³, in which case there would be one or two spent SRFs. TheUF loads only with the colloidal material that passes through the SRF.The expectation is that one spent UF is generated per 5,000 m³ of water.ISM vessels are expected to be spent after five days of operation, thusgenerating 3.33 spent ISM vessels per 5,000 m³ of water.

The MPS has been optimally designed to operate at an operational flowrate of 300 m³/day (55 gpm) (flow rate when system is operating,excludes downtime for filter and media changes, for reconfiguration orrepositioning, for scheduled and unscheduled maintenance, etc.) with astrontium decontamination factor (DF) of greater than 10. The optimizedgoal is a DF of 1,000 which will be achieved under a continuousimprovement program following further operation, assessment, andadjustment.

The process system is designed for ease of transfer to from one site toanother with flexibility for operating in different modes of filtrationand ion removal. Top level process requirements for the inlet waterspecifications are assumed as shown in Table 2.

Top level process requirements for the inlet water specifications areassumed as shown in Table 2.

TABLE 2 Equipment Inlet Water Specifications Unit Range pH 6.6 to 7.1Conductivity μS/cm ≤12,000 Total Na mg/L ≤4,600 Total Mg mg/L ≤400 TotalCa mg/L ≤350 Total Sr mg/L ≤2.3 Total Cl mg/L ≤6,000 Total SO₄ mg/L ≤570Suspended Solids (SS) mg/L ≤20 Total Organic Carbon (TOC) mg/L ≤10Biochemical Oxygen Demand mg/L <1 (BOD) Sr-90 Bq/cc 5E+4 to 4E+5 Total βBq/cc <8E+5 Total γ Bq/cc <300 SS Particle Size Distribution   >1 μm wt% >13 1 μm to 0.01 μm wt % >59 <0.01 μm wt % <1 Sr Activity DistributionIonic % 4 to 8 Particles (>1 μm) % 13 to 37 Particles (<1 μm) % 59 to 79

In an embodiment, the Control/Solids Feed skid 140 (FIGS. 7 and 19) isused to control the feed rate of sorbent to the Feed/Blend skid (FIGS. 8and 20). The Feed/Blend skid 130 (FIGS. 8 and 20) accepts water from thesite at a flow rate of 300 m³ per day (55 gpm). This rate accommodatesthe addition of chemicals in powder form over a range of 100 to 800 kgpowder to 1000 m³ of water with chemical contact time of 40 minutesproviding a continuous flow to the Solids Removal Filter skid 120 (FIGS.9 and 21).

In an embodiment, the Solids Removal Filter skid 120 (FIGS. 9 and 21)accepts water from the Feed/Blend skid (FIGS. 8 and 20) to remove thepowdered sorbent or ion exchange material solids and provides filteredwater to the Ultra Filter skid 110 (FIGS. 10 and 22) achieving anabsolute filtration of 2.0 μm (0.8 μm nominal).

In an embodiment, the Ultra Filter skid 110 (FIGS. 10 and 22) acceptswater from the Solids Removal Filter skid 120 (FIGS. 9 and 21) for theremoval of colloidal solids for providing filtered water to the IonSpecific Media skid 100 (FIGS. 11-12 and 23-24) with a capability ofabsolute filtration of 10,000 Dalton (Da). The Ion Specific Media skid100 (FIGS. 11-12 and 23-24) accepts water from the Ultra Filter skid 110(FIGS. 10 and 22) and is designed to provide a shielded ion-exchangeprocess through a strontium specific granular media, and deliveringprocessed water back to RO reject storage tanks at the rate of 300m³/day.

Water Remediation

Reverse osmosis (RO) is a water purification technology that uses asemipermeable membrane to remove larger particles from drinking water.In reverse osmosis, an applied pressure is used to overcome osmoticpressure. Reverse osmosis can remove many types of molecules and ionsfrom solutions, including bacteria, and is used in both industrialprocesses and the production of potable water. The result is that thesolute is retained on the pressurized side of the membrane and the puresolvent is allowed to pass to the other side. Reverse osmosis is mostcommonly known for its use in drinking water purification from seawater,removing the salt and other effluent materials from the water molecules.Reverse Osmosis is well-known in the art of water remediation, both asan overall process and a highly mobile one. Thus, it is clear that theRO process could be included as a skid within the mobile processingsystem.

Another remediation process is isotope separation via helical screwconveyer. The helical screw ion exchange (HSIX) system transports mediain either a parallel flow or counter-flow configurations wherein thecontaminated water is mixed with ion exchange media to facilitatetransfer of contaminants from the contaminated water yielding cleanwater and a contaminant laden slurry to be processed for furtherdisposition. The HSIX system is detailed in co-pending application No.62/152,521, filed Apr. 24, 2015, entitled HELICAL SCREW ION EXCHANGE ANDDESSICATION UNIT FOR NUCLEAR WATER TREATMENT SYSTEMS, which is hereinincorporated by reference in its entirety. The HSIX system may be usedin place of, or in combination with, the ISM module, and may becontained in a skid for mobile, modular, and scalable operation similarto other skid system components as previously discussed in thedisclosure.

FIG. 25 represents an embodiment of the Pilot skid as a smaller scalecomplete system housing the functionalities as previously described forthe Feed/Blend, Solids Removal Filter, Ultra Filter, and ISM skids in asingle enclosure.

The following is a detail system description of a Pilot skid embodimentcomprising:

-   -   A Feed Preparation and Blending to prepare waste feed for        downstream operations, where the downstream operations include        the steps of:        -   Adding powdered sorbent or ion exchange material to            accurately dose waste water,        -   Mixing waste water and powder in batches up to 500 liters,        -   Sampling waste water before and after powder addition and            mixing, and        -   Delivering feed to downstream processes at a nominal feed            rate of 7.5 liters per minute.    -   A First Stage Filtering        -   Absolute filtration of 2.0 μm (0.8 μm nominal) shall be            achieved        -   Simulate the production scale Solids Retention Filter (SRF)    -   A Second Stage Filtering        -   Absolute filtration of 10,000 Dalton (Da) can be achieved        -   Simulate the production scale Ultra-Filter (UF)    -   An ISM        -   Removal of dissolved strontium        -   Simulation of a production scale ISM    -   A control system for operation of skid equipment    -   Piping, pumps, valves, and instrumentation required to support        pilot operations    -   HVAC to provide a suitable environment for equipment and        personnel    -   Shielding to support operator involvement for routine operations        such as setting valve line ups    -   Small footprint and portability    -   Seismic resistance consistent with the full scale MPS system

The Pilot embodiment utilizes a site interface power is 460 V, 3 phase,50 Hz that is provided to a location near the MPS. Non-potable cleanwater is provided to the MPS site via hoses for system flushing.Alternatively, clean water output from the system may be rerouted backthrough for routine flushing of the system. The flush volume will beapproximately 1900 L (500 gallons). Mobile cranes will be used inroutine production operations to remove and replace filters and ISMs.Process equipment and piping can be arranged to mitigate risk of damagedue to incidental contact during these operations and guard rails and/orstructures shall be provided if indicated.

The clean water exiting the MPS is sampled at various points throughoutthe separate modules to ensure that it meets environmental and healthstandards at the final outlet. Water may be sampled by at least one ofmanually and automatically. In some embodiments, the clean water isstored in storage tanks on site to await further disposition. In someembodiments the clean water is rerouted back through the system forsystem flushing operations.

The Mobile Processing System (MPS) design incorporates applicable codesand standards for the real-time processing of radioactive waste.Considerations for the systems design and equipment will meet or exceed:

-   -   “JSME Nuclear Power Plant Design Standard Design and        Construction Standard” (2005 or later),    -   “JSME Nuclear Power Plant Design Standard Weld Standard” (2005        or later), and    -   “JAEG Nuclear Power Plant Seismic Resistance Inspection        Guideline.”    -   Additional documentation will need to be developed including:        -   “Implementation Plan Application of Special Nuclear Power            Plant Facility”,        -   “Pre Use Inspection” and        -   “Weld Inspection”.

Nominal Materials

Table 3 below lists an embodiment of common equipment specifications.Other equipment specifications are possible.

TABLE 3 Common Equipment Specifications Pressure Rating Operating (at93.3 C. (200 F.) Equipment Wall Thickness Pressure or less) MaterialsPiping, 6.02 mm <1.34 MPa 8.96 MPa 316L SST DN100 (4 in) (0.237 in, Sch40S) (195 psig) (1300 psig) Piping, DN 3.91 mm <1.34 MPa 11.0 MPa 316LSST 50 (2 in) (0.154 in, Sch 40S) (195 psig) (1600 psig) Piping, DN 3.38mm <1.34 MPa 19.3 MPa 316L SST 50 (1 in) (0.133 in, Sch 40S) (195 psig)(2800 psig) Piping, DN 2.87 mm <1.34 MPa 24.1 MPa 316L SST 20 (¾ in)(0.113 in, Sch 40S) (195 psig) (3500 psig) Tubing, 19 mm 1.24 mm <1.34MPa 11.0 MPa 316L SST (¾ in) (0.049 in) (195 psig) (1600 psig) Tubing,13 mm 0.89 mm <1.34 MPa 12.4 MPa 316L SST (½ in) (0.035 in) (195 psig)(1800 psig) Pipe Flanges Varies <1.34 MPa 1.34 MPa 316L SST (195 psig)(195 psig) Pumps Varies <1.34 MPa 2.50 MPa Housing: CF8M SST (195 psig)(363 psig) Impeller: 316 SST Feed/Blend Upper Shell: 7.94 mm <1.34 MPa−0.072 MPa to 316L SST Tanks ( 5/16 in) (195 psig) 0.128 MPa LowerShell: 7.94 mm (−10.4 psig to ( 5/16 in) 18.5psig) Top Head: 51 mm (2in) Bottom Head: 6.35 mm (¼ in) Solids Top Head: 4.76 mm <1.34 MPa 0.52MPa 316L SST Removal ( 3/16 in) (195 psig) (75 psig) Filters Shell: 6.35mm (¼ in) Bottom Head: 4.76 mm ( 3/16 in) Ultra Filters Top Head: 4.76mm <1.34 MPa 2.07 MPa 316L SST ( 3/16 in) (195 psig) (300 psig) Shell;6.35 mm (¼ in) Bottom Head: 4.76 mm ( 3/16 in) Ion Specific Top Head:44.5 mm <1.34 MPa 0.97 MPa 316L SST Media (1¾ in) (195 psig) (140 psig)Vessels Shell: 9.53 in (⅜ in) Bottom Head: 44.5 mm (1¾ in) fprojectVaries <1.34 MPa Flowtek: 1.72 MPa CF8M (195 psig) (250 psig) SST/UHMWPESwagelok: 10.3 MPa (1500psig) Pressure Varies <1.34 MPa 1.34 MPa CF3MSST Relief Valves (195 psig) (195 psig) Hoses 10.9 mm <1.34 MPa 1.72 MPaTube: Black Nitrile (0.43 in) (195 psig) (250 psig) synthetic rubber(Class A oil resistance) Cover: Black Chemivic ™ synthetic (corrugated)(vinyl reinforced nitrile) Reinforcement: Spiral-plied synthetic fabricwith wire helix

With a discussion now on materials selection and corrosion resistance,dual certified 316/316L stainless steel was selected for tanks and 316Lfor piping that will provide containment of tank water being processed.The quick letter water chemistry specification was used to evaluateanticipated bounding levels of chloride, conductivity and ionic contentin tank water. 316L was selected because it is rated for use in thisenvironment and is readily available. To further reduce the risk ofcorrosion the material will be passivated with nitric acid prior todelivery. Pipe spools will have welds cleaned and then the entire pipespool will be passivated again after fabrication. Tank welds will beindividually cleaned and passivated after fabrication.

Pumps will be made from 316L with impellers having a smooth finish thatwill reduce corrosion. Valve bodies will be composed of CF8M steel thatis rated for seawater use. Kamvelok connectors will be composed of CF3Msteel that is rated for seawater use.

304L stainless steel will be used for drip pans and structural steelthat will not contact tank water. This material provides generalenvironmental corrosion resistance, is readily available and has lowercost than 316/316L.

Considerations for radiation resistance have been incorporated byselecting polymer materials for use in the MPS, these are shown belowwith published radiation damage thresholds identified. Soft seats arepreferred in valves to ensure leak tightness. Hoses were selected forpressure rating, bend radius, weight, and ease of handling. Theseproperties are important to the process, but radiation resistance wasemphasized in material selection. Fluoroelastomers (eg PTFE, Teflon) arecommon valve seat materials but were avoided due to their recognized lowtolerance to radiation exposure.

TABLE 4 Radiation Resistance of Materials Approximate Damage MaterialUse in MPS Threshold (Gy) UHMWPE Ball valves 1 × 10⁴ to 5 × 10⁵ EPDMKamvaloks, check valves, surge 5 × 10⁵ to 1 × 10⁶ suppressors EPRPressure relief valves 5 × 10⁵ to 1 × 10⁶ Nitrile Rubber Hoses 1 × 10⁶

Further, structural strength and seismic safety are included in Tables5, 6, and 7. Below.

TABLE 5 Structural Strength Results of the MPS Vessels Required MaximumMaximum Thickness Internal Required External for Working Thickness forWorking External Actual Equipment Assessed Pressure Internal PressurePressure Thickness Name Part (MPa) Pressure[mm] (MPa) (mm) [mm] ISMVessel Plate 0.986 5.3 Does not apply to this 9.5 thickness vesselFeed/Blend Plate 0.128 2.9 0.072 3.8 7.9 Vessel Thickness 3.1 3.8 7.92.0 3.0 7.9

TABLE 6 MPS's Seismic Safety Assessment Results Horizontal EquipmentAssessed Assessment Seismic Calculated Allowable Name Part itemCoefficient Value Value Unit Feed Blend Main Overturn 0.36 290 341 kN ·m Skid body UF Skid 355 454 SRF Skid 355 454 ISM Skid 288 398 Controland Solids Feed Skid

TABLE 7 Results of the Pipes' Structural Strength Assessment MaximumMaximum Working Working Required Actual Assessed Pressure TemperatureThickness Thickness Part Diameter Sch. Material (MPa) (C.) (mm) (mm)Pipe (1) 2″ 40S JIS G 3459 1.03 66 0.5 3.9 316LTP Pipe (2) 4″ 40S JIS G3459 1.03 66 0.8 6.0 316LTP

Since radiation protection is of paramount importance, filters and ISMvessels that accumulate radioactive material are enclosed in shielding.The SRF and UF filters are enclosed in 51 mm of shielding carbon steeland the ISM vessels have 25 mm of carbon steel shielding. Dose ratecalculations have been performed and the goal is to limit on-contactdose rates to 5 mSv/hr. Dose calculations were based on a source termtwo standard deviations above the average source term fromcharacterization data and fully loaded filter cartridges. Calculateddose rates are shown in the table below. Each vessel will have aradiation monitoring probe and operating areas will have general arearadiation monitors. Radiation detection will be monitored at both thelocal control skid and remote monitoring station.

TABLE 8 Radiation Shielding Specifications Shielding Thickness ContactDose Rate Feed/Blend Tank  0 mm (0 in) 0.24 mSv/hr  Solids RemovalFilter 51 mm (2 in) 1.4 mSv/hr Ultra Filter 51 mm (2 in) 4.8 mSv/hr ISMVessels 25 mm (1 in)   9 mSv/hr

Temperature control for spent SRFs, UFs, and ISM vessels caused byself-heating due to captured Sr-90 along with the result of MPSoperation have been considered. The self-heating from the Sr-90collected in an SRF filter (21.5 watts), the Ultra Filter (249.4 watts),and the ISM vessel (1.3 watts) has been evaluated. When ambienttemperature is 40° C., the following results are obtained for thetemperature of shielding exposed to ambient air, and for the internalfilter canisters in wet and dry storage, and for ISM vessels in drystorage:

-   -   Solids Removal Filter        -   Shielding temperature exposed to ambient conditions 41.75°            C.        -   Canister centerline temperature dry storage not more than            63.8° C.        -   Canister centerline temperature wet storage not more than            47.3° C.    -   Ultra Filter        -   Shielding temperature exposed to ambient conditions 52.4° C.        -   Canister centerline temperature dry storage not more than            106.3° C.        -   Canister centerline temperature wet storage not more than            87.4° C.    -   ISM        -   Shielding temperature exposed to ambient conditions 40.22°            C.        -   ISM bed centerline temperature not more than 43° C.

When spent filters and ISM vessels are stored in the sun, there ispotential for additional heating of external surfaces due to solarradiation. Heating by solar radiation was not included in the abovecalculations. The precise amount of heating from solar radiation isdifficult to assess because it is highly dependent on weatherconditions. When incident solar radiation is 700 watts per m², and thereis a moderate wind of 5 m/s, plate metal can heat to 19° C. aboveambient temperature. When the wind is 1 m/s, plate metal may heat to 37°C. above ambient air temperature. Similar increases in canistercenterline temperature can be expected since the internal heating mustnow dissipate through the shielding that is solar heated as well asbeing heated from inside. These temperatures will not compromise thecontainment boundary provided by the filter canisters or the ISM vessel.The heat from all the Sr-90 stored in the process when water is flowingat 208 L/min will raise the temperature of the water by 0.019° C. Whenflow is interrupted, the UF canisters heat at 13° C./day and SRFcanisters heat at a rate of 0.89° C./day.

Leak Prevention/Environmental Considerations/Safety

The system is designed so as to prevent leaks, damage to theenvironment, and injury to on-site operators.

In an embodiment, the system design includes a local control room andcommunication for remote operations during normal run time andinterconnections between MPS units that are integrated into the controlsystem allowing all system operations to be performed by the centralcontrol station. Further this allows immediate response to conditionswith pump shutdown or failure guaranteeing unit isolation as needed tosatisfy leak and radiological protection requirements.

Additional considerations for the pilot embodiment can be made to reducethe radioactive operator dose by installing shield, maintenancefrequency reduction, radiation monitoring, and installation of theremote operation.

The design prevents the radioactive material from leaking to theenvironment; however, should any radioactive material be released fromthe train, the dam installation, leak detector installation, and pipinginstalled outside the building, etc. has been designed to prevent anyleaked radioactive material from defusing, to include leak protection ofthe joints etc. All process lines between skids consist of hoses withsecondary containment for the prevention of spills to the environment.All filter vessels are provided with adequate shielding.

Check valves are used through the system to prevent flow from flowingbackwards. Many of the valves are motor operated to allow for quickshutoff or open as necessary to prevent leaks or reduce pressure. Allpressure gauges in the system display locally and most display in thecontrol room as well for careful monitoring of system pressure. Pressurerelief valves are located in each skid to automatically release pressurewhen the system pressure exceeds a predetermined value. The motoroperated valves are designed to fail as-is, open, or closed depending ontheir location in the system to minimize damage and environmentalhazards in the event of failure. Redundant valves are used throughoutthe system to provide additional control and increase the factor ofsafety of the system, again reducing the possibility of leakage to theenvironment in the event of a failure. Instrument interlocks are used toprevent operators and/or machinery from being harmed in the event of aleak or other failure.

In an embodiment, process equipment and piping can be arranged tomitigate risk of damage due to incidental contact during theseoperations and guard rails and/or structures shall be provided ifindicated. Additionally, seismic resistance is consistent with the fullscale MPS system.

Further, the design prevents the retention of flammable gas if suchretention is a matter of concern. Hydrogen control is a concern from anexplosion hazard; therefore a hydrogen venting capability is provided.The approach to controlling hydrogen in the MPS is based on dilution toprevent a hydrogen concentration in air from exceeding a lowerflammability limit (LFL). When connected to the process system thefilters will have vent line with inert gas purge capability to safelyvent hydrogen out of the ISO container. For filters in storagecalculations and testing of filter characteristics needed to demonstratethat passive venting of the filters will effectively control hydrogenhave not been completed. Active venting by forced air circulationsimilar to the vacuum pumping initially used on the cesium ISM vesselsmay be required until effectiveness of passive venting is demonstrated.

In an embodiment, the instrumentation and control systems are designedto provide for fully automatic normal operations of the system throughthe use of fully redundant fault tolerant programmable logic controllers(PLC); any off-normal operations are not automatically controlled,however the system implements a “graceful” shut down with provision formanual intervention at any point in the process cycle. The system designincludes a local control room and communication for remote operationsduring normal run time and interconnections between MPS units that areintegrated into the control system allowing all system operations to beperformed by the central control station. Further this allows immediateresponse to conditions with pump shutdown or failure guaranteeing unitisolation as needed to satisfy leak and radiological protectionrequirements.

Stacking

In some embodiments skids may be stacked on top of other skids to reducesystem footprint. The depicted configurations, FIGS. 26A-26D are exampleembodiments using twenty foot standard intermodal shipping containers.Hatching within the depicted figures indicates containers that are incontact with the ground. Example stacking embodiments as shown depictcontainers stacked two-high. Additional stacking configurations, notshown, are possible, including stacking of three or more skids high.Other skid sizes may be used. Additionally, configurations involving twoor more differently sized skids are possible, for instance: a forty footintermodal container stacked on top of two twenty foot intermodalcontainers. In some embodiments, additional structural supports,coupling mechanisms, and/or access points are included in anticipationof various stacking configurations.

Elevated access platforms may be installed to allow disconnect offilters and ISM vessels for replacements, hydrogen venting, sampling,access to the control room, and placement of interconnecting hoses.Crane access may be required for routine operational replacement ofsolids removal filters, ultra filters, and ISM vessels. Alternatively,openings in the sidewalls, roofs, and/or floors of the skids, with orwithout doors, may be provided to afford access to filters and ISMvessels for the purpose of routine operational replacement.

FIG. 27 depicts an example embodiment wherein a Control and Solids Feedskid 140 is stacked on top of a Feed/Blend skid 130 and a Solids RemovalFilter skid 120. In the depicted embodiment, the feed side of theControl and Solids Feed skid 140 may be situated atop the Feed/Blendskid 130 wherein the solids may be fed via gravity through the floor ofthe Control and Solids Feed skid 140 directly into the Feed/Blend skid130. The control side of the Control and Solids Feed skid 140 may besituated above the Solids Removal Filter skid 120. The Solids RemovalFilter skid 120 may be situated so as to allow easy access to thefilters from the top of the skid. The control room may be accessible topersonnel by ladder or stairs (not shown).

For the sake of convenience, the operations are described as variousinterconnected functional blocks or distinct software modules. This isnot necessary, however, and there may be cases where these functionalblocks or modules are equivalently aggregated into a single logicdevice, program or operation with unclear boundaries. In any event, thefunctional blocks and software modules or described features can beimplemented by themselves, or in combination with other operations ineither hardware or software.

Having described and illustrated the principles of the invention in apreferred embodiment thereof, it should be apparent that the inventionmay be modified in arrangement and detail without departing from suchprinciples. Claim is made to all modifications and variation comingwithin the spirit and scope of the invention as claimed.

1. A modular nuclear waste processing method, comprising: configuringtwo or more process modules, to provide scalability andreconfigurability, wherein scalability and reconfigurability areachieved by the use of at least one of standardized connections anddimensionally standardized process modules, and wherein the modularnuclear waste processing system is further configured to: monitorchemical properties of nuclear process waste water input to a firstprocess module, wherein the monitoring is at least one of manual andautomatic, wherein the first process module is configured to mix ametered quantity of a sorbent into the nuclear process waste water,wherein the metered quantity is determined stoichiometrically based onthe monitored chemical properties of the nuclear process waste water,and wherein the metered quantity is one of manually and automaticallyfed into the system; monitor the chemical properties of the sorbenttreated water at an outlet from the first process module, wherein themonitoring is at least one of manual and automatic; responsive to themonitored chemical properties of the sorbent treated water adjust themetered quantity of the sorbent; feed the sorbent treated water from thefirst process module outlet to a second process module, wherein thesecond process module comprises one or more vessels containing ionexchange media; monitor the chemical properties of the water at anoutlet from the second process module wherein the monitoring is at leastone of manual and automatic; and responsive to the monitored chemicalproperties of the water at the outlet from the second process module,one of confirm and fine-tune the metered quantity of sorbent.
 2. Themethod of claim 1, wherein the method further comprises one or moreprocess modules operative to process contaminants removed from thenuclear process waste water.
 3. The method of claim 1, wherein one ofthe one or more process modules is operative to vitrify the contaminantsremoved from the nuclear process waste water.
 4. The method of claim 1,wherein two or more of the process modules are placed at differentelevations.
 5. The method of claim 1, wherein the capabilities of two ormore process modules are contained in a small scale pilot processmodule.
 6. The method of claim 1, wherein the one or more processmodules are contained in intermodal containers.
 7. The method of claim1, wherein the sorbent is at least one of bead form and granular.
 8. Themethod of claim 1, wherein sorbent quantity is adjusted to normalize theconcentration of a specific ion such that the chemical conditions remainstable.
 9. The method of claim 1, wherein the time to bind the sorbentto contaminants in nuclear process waste water is dependent upon atleast one of the ion and an isotope to be treated.
 10. The method ofclaim 1, wherein key components are set for automatic response in theevent of a failure, exceeded temperature, pressure, and radiationranges, and other phenomena requiring system shutdown.
 11. The method ofclaim 1, wherein the one or more of the process modules comprise one ormore motor operated valves at each end of at least the primary lines tocontrol flow rates in and out of the process modules.
 12. The method ofclaim 11, wherein the one or more motor operated valves are furtheroperative to one of manually and automatically open to reduce pressureand close to stop system flow in the event rapid system shutdown isrequired.
 13. The method of claim 1, wherein redundant valves areimplemented in the one or more process modules to increase the factor ofsafety of the system.
 14. The method of claim 1, wherein two or moreprocess modules are connected in series.
 15. The method of claim 1,wherein two or more process modules are connected in parallel.
 16. Themethod of claim 1, wherein two or more process modules are connected inseries and further in parallel to two or more additional processmodules.